Method and apparatus for extracting botanical oils

ABSTRACT

Various aspects of the disclosure relate to methods and systems for extracting oil from plant material. A system may comprise a gas moving device, an extraction chamber, and a condensation surface. Oil of the plant material may be volatized in the extraction chamber and then propelled by the gas moving device to the condensation surface to be collected. In various embodiments, the systems and methods allow the extraction of oil from plant material with little or no solvent.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a continuation of prior application Ser. No.16/098,265, filed Nov. 1, 2018, which granted as U.S. Pat. No.10,617,974, which is the U.S. national phase under 35 U.S.C. § 371 ofInternational Application No. PCT/US2017/030557, filed May 2, 2017,which claims priority to U.S. Provisional Patent Application No.62/330,522, filed May 2, 2016, and the entire contents of each of thepreceding applications are incorporated by reference in its entirety.

SUMMARY OF THE INVENTION

The present invention consists of a system of parts and processes thatare used to extract botanical oils, terpenoids, oleoresins and/or resins(generically referred to in this disclosure as “oils” or “plant oils”)from plant material or an oil containing substrate (generically referredto in this disclosure as “plant material”). The method of extractionincludes contacting the plant material with a heated gas and/or heatedsurface of a specific temperature such that the oils contained withinthe plant material are caused to volatilize and leave the plant materialin the form of a vapor. The vapor is then condensed and collected usinga collection solvent in a manner that preserves and protects theintegrity of the oil constituents. The collection solvent utilized inthe system is preferably ethanol or a mixture of ethanol and water,however, water, chloroform or a number of other suitable organic orinorganic solvents may be utilized to attain the desired results. Amethod of separating the captured plant oils from the collection solventis included whereby a substantially purified plant oil extract can beobtained as a final product of the system.

As non-limiting examples, a few of the many types of plant materialsthat may be processed using the present invention may include variousforms of hemp or cannabis that may generally be classified as Cannabissativa, Cannabis indica, Cannabis ruderalis, hybridized crosses ofvarious species or families of cannabis, or a mixture of one or moretypes of cannabis and/or other plant material. When cannabis is selectedas the plant material to be processed, the preferred oils to beextracted may include the various chemical forms of cannabidiol (“CBD”),cannabidivarin (“CBDV”), delta-9-tetrahydrocannabinol (“THC”),delta-8-tetrahydrocannabinol, tetrahydrocannabivarin (“THCV”),cannabinol (“CBN”), cannabigerol, cannabichromene, chemically convertedcannabinoids or any other cannabinoid. Other valuable terpenoid oilsthat may be extracted from cannabis may include the various chemicalforms of linalool, caryophyllene, myrcene, limonene, humulene, pinene.By manipulating the temperature of the heated gas and/or heated surfacesthat contact the plain materials and completing successive extractioncycles, it is possible to isolate the various plant oils intosubstantially purified fractions. It is also possible utilize a widertemperature band to extract a range of plant oils in a single extractioncycle. It should be noted that any plant material may be processed bythe present invention and any plant oils may be targeted as the oils tobe extracted.

An embodiment of the present invention provides a system for extractingan oil from plant material. A gas moving device is operable to propel agas stream through the system, the gas stream being a stream of air orgas with or without entrained vapor, solids or droplets of liquidtherein. An extraction chamber is in communication with the gas movingdevice such that the gas stream is directed through the extractionchamber, the extraction chamber operable to volatize at least a portionof an oil from a plant material such that the volatilized oil isdisposed in the gas stream as an extracted oil. A collection chamber isin communication with the extraction chamber such that the gas streamflows through the collection chamber, the collection chamber havingcollection solvent operable to collect at least a portion of theextracted oil from the gas stream. A liquid collector in fluidcommunication with the collection chamber for collecting at least aportion of the collection solvent and extracted oil.

Some versions include a heater disposed such that the gas stream flowsthrough the heater and the gas stream is heated. The heater may beoperable to heat the gas stream to a temperature sufficient to causevolatilization of the oil to be extracted, with the extraction chamberbeing in communication with the heater such that the heated gas streamis directed through the receiving area, the extraction chamber operableto volatilize the portion of the oil by the heated gas streamvolatilizing the portion of the oil as the heated gas stream flowsthrough the extraction chamber. The extraction chamber may include avolatilization chamber having an upwardly facing entry tube and an exitdisposed below the entry tube such that the gas flow impacts an upperend of the volatilization chamber and reverses direction before exitingthe volatilization chamber. The extraction chamber may be a modifiedspray dryer having a nozzle, the heated gas stream with entrained plantmaterial being introduced through the nozzle. In some examples, theheater is operable to heat the gas stream at an exit of the heater or inthe extraction chamber to a temperature in the range of 290 to 430degrees Fahrenheit. In certain examples, the heater is operable to heatthe gas stream to a temperature of at least 290 degrees Fahrenheit. Theheater may be a tube-in-shell heat exchanger with a steam generatorproviding steam to the heat exchanger or is an electric heater.

In some versions, the extraction chamber includes a volatilizationchamber having at least one heated surface and the portion of the oil isvolatilized by the plant material contacting the heated surface. Incertain examples, the at least one heated surface has a temperature isin the range of 290 to 430 degrees Fahrenheit. In some examples, the atleast one heated surface has a temperature of at least 290 Fahrenheit.The extraction chamber may have a tangential entrance.

In some versions, the extraction chamber includes a flash dryingvolatilization chamber having an entrance and an exit, the exit beingabove the entrance such that the gas stream flows upwardly and entrainedplant materials are carried upwardly by the gas stream. The entrance maybe a nozzle.

In some embodiments, the extraction chamber comprises a volatilizationchamber having a tangential entrance.

In some versions, the extraction chamber includes elements to break upclumps of plant material. Examples of such elements include balls, beadsand rotating elements.

In some embodiments, the extraction chamber includes an insulated and/orheated shell.

In certain versions, the extraction chamber may include a plurality ofvolatilization chambers in series and/or parallel.

Some versions of the extraction chamber may have a receiving area forreceiving plant material for extraction.

Certain embodiments further include a plant material entrainment zone incommunication with the gas stream mover such that the gas stream flowsthrough the plant material entrainment zone, the plant materialentrainment zone forming at least a part of the extraction chamber. Ahopper for holding plant material and a plant material portioning deviceoperable to introduce the plant material into the plant materialentrainment zone may also be included. Examples of the plant materialportioning devices include an auger screw, a rotary valve, and a rotaryairlock valve.

In some embodiments, the collection chamber has at least one collectionsolvent sprayer operable to spray droplets of collection solvent intothe gas stream such that at least some of the extracted oil dissolvesinto the collection solvent droplets and at least some of the collectionsolvent droplets flow to the liquid collector. The at least onecollection solvent sprayer may be a plurality of collection solventsprayers and the collection solvent droplets may generally have adiameter greater than one micron and less than 300 microns. Thecollection chamber may have packing material disposed therein with thepacking material wetted by the collection solvent.

In some embodiments, the system includes a secondary liquid separator incommunication with the collection chamber.

In certain embodiments, the system includes a cooling chamber incommunication with the extraction chamber such that the heated gasstream flows through the cooling chamber, and the cooling chamber isoperable to cool the heated gas stream to or below a volatilizationtemperature of the extracted oil such that at least some of theextracted oil liquefies into droplets entrained in the gas stream. Thecollection chamber is downstream of the cooling chamber. The coolingchamber may be a spray cooling chamber having a high pressure sprayeroperable to spray collection solvent into the heated gas stream suchthat the collection solvent rapidly cools the heated gas stream to orbelow a condensation temperature of the oil. The sprayed collectionsolvent may be collection solvent and extracted oil from the liquidcollector, and the system may further include a pump operable to pumpthe collection solvent and extracted oil from the liquid collector tothe high pressure sprayer. Alternatively, the sprayed collection solventis a substantially purified collection solvent. A collection solventcooler may be provided to cool the collection solvent for the highpressure sprayer.

In certain embodiments, interior surfaces of the extraction chamber andportions of the system downstream of the extraction chamber and upstreamof the collection and/or cooling chamber are maintained at a temperaturesufficient to prevent condensation of the volatilized oils on saidinterior surfaces. In some examples, the temperature sufficient toprevent condensation is in the range of 290 to 430 degrees Fahrenheit.

Some embodiments include a gas stream cooler in communication with theextraction chamber. The gas stream cooler may be a tube-in-shell heatexchanger.

Some embodiments include an agglomeration chamber in communication withthe cooling chamber or extraction chamber so as to receive the gasstream, the agglomeration chamber increasing the droplet size in the gasstream. The agglomeration chamber may have a diameter greater than adiameter of a passage upstream of the agglomeration chamber such thatthe gas stream slows down in the agglomeration chamber. Theagglomeration chamber may include at least one collection solvent vaporinjector operable to introduce a collection solvent vapor to theagglomeration chamber. Alternatively, or additionally, the agglomerationchamber may have a flow of cool gas that mixes with the heated gasstream. An oil/solvent separation system may be provided to generallyseparate the collection solvent from the extracted oil so as to providea generally purified collection solvent and a generally purified oil,with the separation system providing collection solvent vapor to the atleast one collection solvent vapor injector.

In some embodiments, passages or chambers disposed downstream of theextraction chamber have inner surfaces with a temperature less than acondensation temperature of the collection solvent such that collectionsolvent vapor entrained in the gas stream condenses on the innersurfaces and forms a solvent liquid that washes accumulated oils andcollection solvent containing dissolved oils from the inner surfaces,the combined liquid flowing to the liquid collector. In certainexamples, the temperature less than a condensation temperature is in therange of approximately 85 to 145 degrees Fahrenheit. In some examples,interior surfaces of the extraction chamber are heated to a temperaturesufficient to prevent condensation of the volatilized oils on theinterior surfaces.

Some embodiments include an oil/solvent separation system operable togenerally separate the collection solvent from the extracted oil toprovide a generally purified collection solvent and a generally purifiedoil. The separation system may include an evaporation device, and mayalso include a condenser to condense solvent vapor from the evaporationdevice.

Some embodiments include a plant material separation device incommunication with and downstream of the extraction chamber, the plantmaterial separation device operable to separate at least a portion ofthe plant material entrained in the gas stream therefrom. The plantmaterial separation device may be a cyclone or centrifugal separatorand/or the separator has a heated exit and/or the separator has a heatedbackflow to displace vapors. The plant material separation device mayalso include a secondary entrainment zone and a secondary gas streammover operable to propel a secondary gas stream through the secondaryentrainment zone, the plant material separation device providing theseparated portion of plant material to the secondary entrainment zone. Asecondary plant material separator may be in communication with thesecondary entrainment zone. In some examples, the secondary gas streamhas a temperature less than a temperature of the gas stream flowingthrough the plant material separation device. A gas stream filter may bein communication with the plant material separation device.

Some embodiments include a collection solvent separation device forseparating at least a portion of the collection solvent from the gasstream.

Certain embodiments include a gas pump operable to remove gas from thesystem so as to maintain an interior pressure below atmospheric andprevent outward leakage from the system.

In some examples, the collection solvent is: a non-toxic, food-gradesolvent; a mixture of ethyl alcohol and water; a mixture of organicethyl alcohol and water; or a solvent containing at least 40% ethylalcohol. In further examples, the collection solvent is ethanol, amixture of ethanol and water, water, chloroform or organic or inorganicsolvents.

In some embodiments, at least a portion of the collection solvent andextracted oil is recirculated to the collection chamber.

In certain embodiments, the plant materials are raw plant portions orpartially processed plant portions and the extracted oil includesterpenoids.

In certain embodiments, the system is a substantially closed loopsystem.

In some versions, the liquid collector is a sump in fluid communicationwith at least the collection chamber.

In certain embodiments, the plant materials are raw plant portions orpartially processed plant portions and the system is extracting one ormore specific saps, resins, oleoresins, lipids, terpenoids or otherwisevolatilizable constituents within a plant material that is beingprocessed.

In some embodiments, the gas stream includes a gas selected from air,inert gas, reducing gas and mixtures thereof.

The gas stream mover may be a blower.

The present invention also includes use of any apparatus describedherein to provide an extracted oil.

In some versions, the gas moving device is part of the collectionchamber.

In some embodiments, the heater and/or the plant material separatorand/or the gas stream filter 49 and/or the extraction chamber areinsulated and/or heated.

The present invention includes a method for extracting an oil from plantmaterial. Any system described herein may be used. A plant material isprovided in the extraction chamber and oil is volatilized from the plantmaterial, the oil being extracted into the gas stream. The gas stream iscontacted with a collection solvent such that at least some of the oilis captured by the collection solvent. At least a portion of the oil andcollection solvent is collected from the gas stream. In some versions,the plant material is exposed to the heated gas stream, the gas streambeing heated to a temperature sufficient to cause volatilization of anoil to be extracted from the plant material.

In some versions of the method, the contacting and collecting stepscomprise flowing at least a portion of the gas stream through acollection chamber and spraying the at least a portion of the gas streamwith collection solvent such that at least some of the oil in the gasstream is captured by the collection solvent and at least some of thecollection solvent flows to the collection chamber.

In some versions of the system or method the plant material is one ormore types of cannabis. In some versions, the extracted oil contains oneor more of: cannabidiol (“CBD”); cannabidivarin (“CBDV”);delta-9-tetrahydrocannabinol (“THC”); delta-8-tetrahydrocannabinol;tetrahydrocannabivarin (“THCV”); cannabinol (“CBN”); cannabigerol;cannabichromene; chemically converted cannabinoids; or othercannabinoids.

In some versions of the system or method, the extraction chamber isoperated at a temperature of approximately 315 degrees Fahrenheit.

In some versions of the system or method, the extraction chamber isoperated at a temperature of approximately 356 degrees Fahrenheit.

In some versions of the system or method, the extraction chamber isoperated at a temperature of approximately 428 degrees Fahrenheit.

Further embodiments and options are described throughout thisdisclosure.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a diagrammatic view of an embodiment of the present invention;

FIG. 2 is a diagrammatic view of an alternative embodiment of thepresent invention;

FIG. 3 illustrates an embodiment of a volatilization chamber designed toexpose plant material entrained in the primary gas stream to ahighly-turbulent and highly-agitative environment to facilitate rapidvolatilization of plant oils contained within the plant material;

FIG. 4 illustrates an embodiment of the volatilization chamber that isalso designed to expose the plant material entrained in the primary gasstream to a highly-turbulent and highly-agitative environment tofacilitate rapid volatilization of the plant oils contained within theplant material;

FIG. 5 illustrates an embodiment of the volatilization chamber that isdesigned to centrifugally force the plant material into contact with theheated walls of the volatilization chamber to induce rapidvolatilization of the plant oils;

FIG. 6 illustrates an embodiment of the volatilization chamber thatutilizes a modified form of pneumatic flash drying to induce rapidvolatilization of oils within the plant material;

FIG. 7 illustrates an embodiment of the volatilization chamber that isdesigned to prevent plant material that is still heavily laden with oilsor has clumped together from escaping the volatilization chamber untilit has been broken up into small particles and fully stripped of itsdesirable oils;

FIGS. 8a and 8b illustrate a cross-sectional and a top view of anadditional embodiment of the volatilization chamber that is designed toprevent plant material that is still heavily laden with oils or hasclumped together from escaping the volatilization chamber until it hasbeen broken up into small particles and fully stripped of its desirableoils;

FIG. 9 is a detailed view of a primary plant material separation deviceand a secondary plant material entrainment section, for use with someembodiments; and

FIG. 10 illustrates an embodiment that utilizes a collection chambercontaining wetted packing.

FIG. 11 illustrates a simplified embodiment that uses little or nosolvent.

FIG. 12a illustrates an additional embodiment that uses little or nosolvent and utilizes a centrifugal oil droplet separator.

FIG. 12b illustrates an embodiment that uses little or no solvent andutilizes a centrifugal blower as a centrifugal oil droplet separator.

FIG. 13 illustrates an embodiment that uses little or no solvent andalso facilitates continuous fractionation of the plant oils beingextracted.

FIG. 14 illustrates an embodiment that uses little or no solvent,facilitates continuous fractionation of the plant oils being extractedand utilizes a centrifugal oil droplet separator.

FIG. 15 illustrates an embodiment that uses little or no solvent,facilitates continuous fractionation of the plant oils being extractedand utilizes a centrifugal gas mover as an oil droplet separator.

FIG. 16 illustrates an embodiment that uses little or no solvent andutilizes electrostatic collection plates to facilitate removal of plantoils from the gas stream.

FIG. 17 illustrates an embodiment that uses little or no solvent andutilizes demisting pads and/or packing material to facilitate removal ofplant oils from the gas stream.

DETAILED DESCRIPTION OF THE INVENTION

FIG. 1 illustrates a diagrammatic view of the primary system parts of anembodiment of the present invention. A system is provided that includesa substantially closed network of passages and chambers containing amoving primary gas stream 1 (generically referred to in this disclosureas the “primary gas stream” or “primary gas flow”), a primary gas streamheater 2, a steam generator 3 to provide a heat source to the primarygas stream heater 2, a plant material or oil containing substrate hopper4, a plant material portioning device 5, a primary plant materialentrainment zone 6, a plant material volatilization chamber 7, a primaryplant material separation device 8, an optionally heated separated plantmaterial exit 44, a gas stream filter 49, a cooling and condensationsection 9 for contacting the primary gas stream with a coolingcollection solvent spray 10, a solvent spray cooler 11, a gas streamcooler 50, a primary pump 12 to provide pressurized collection solventto various parts of the system, a sump area 13 to store collectionsolvent and separate collection solvent from the gas stream, anagglomeration chamber 14, a collection solvent vapor/steam introductionmethod 15, a collection chamber 16 for contacting the primary gas streamwith a pressurized spray of collection solvent 17, a separation deviceor chamber 18 to remove a portion of the collection solvent spray fromthe primary gas stream 1, a primary gas stream mover 19, a collectionsolvent droplet separation device 20, a primary gas streamdemister/polishing device 21, a collection solvent condenser 22, anout-only check valve 23 allowing gas to pass from the collection solventcondenser to the atmosphere, an air pump 24 capable of removing aportioned amount of gas from the system, a secondary gas stream 25(generically referred to in this disclosure as the “secondary gasstream” or “secondary gas flow”), a secondary gas stream mover 26, asecondary plant material entrainment zone 27, a secondary plant materialseparation device 28, a processed plant material collection bin 29, anin-only check valve 30 to allow atmospheric air or a displacing gas intothe system via the plant material collection bin 29, a thin filmevaporator 31 or similar rapid evaporation device and a plant oilextract/final product collection container 32. Depending on the desiredapplication, any of these components and parts may be duplicated withinthe system one or more times in series or in parallel or may eliminatedentirely to attain different effects. The order of the components withinthe system may also be modified to attain different effects.

The primary gas stream 1 is propelled through the system by the primarygas stream mover 19. The primary gas stream may consist of atmosphericair, an inert gas such as but not limited to nitrogen, a reducing gassuch as but not limited to CO₂ or any other suitable gas or mixture. Theprimary gas stream mover 19 is preferably a regenerative blower, turboblower, pressure blower or other form of centrifugal blower, however,the primary gas stream mover may consist of any mechanism or methodcapable of moving a gas. The gas stream may be kept above, below orequal to atmospheric pressure as required for different applications oreffects. As the primary gas stream moves through the system, it passesthrough the primary gas stream heater 2. The primary gas stream heateris preferably a tube-in-shell heat exchanger that receives its heat inthe form of saturated steam of a specific pressure and temperatureprovided by a steam generator 3 system, however, dry steam, a heated gasor other forms of heat exchange may be used, including but not limitedto utilizing a hot oil or thermal fluid system whereby a heated fluid ispumped through the heat exchanger. Other forms of steam, gas or fluidpowered heat exchangers may also be used as the application requires.Alternatively, the primary gas stream heater may use electric heatingelements of various designs to heat the gas stream, including, but notlimited to, star-wound heating coil designs. As the primary gas streampasses through the primary gas stream heater 2, the primary gas streamis heated to a temperature that is suitable to volatize one or more ofthe plant oil constituents present in the plant material.

After being heated, the primary gas stream 1 passes through a primaryplant material entrainment section 6 of the system. The plant materialsupply is located in a hopper section 4 of the system. A portionedamount of plant material is introduced to the primary plant materialentrainment section 6 via an auger screw, a rotary valve, a rotaryairlock valve or any other suitable distribution mechanism 5. The plantmaterial is preferably introduced to the system in a finely shredded orpowdered form, however, other consistencies may also be used dependingon what is most preferable in different applications. The plant materialmay be ground to the ideal or suitable consistency externally, or anintegral grinder may be incorporated into the hopper 4, portioningdevice 5 or entrainment section 6 system as described in, but not in anyway limited by, PCT/IB2014/002383. As non-limiting examples, a few ofthe many types of plant materials that may be processed using thepresent invention may include various forms of hemp or cannabis that maygenerally be classified as Cannabis sativa, Cannabis indica, Cannabisruderalis, hybridized crosses of various species or families ofcannabis, or a mixture of one or more types of cannabis and/or otherplant material. It should be noted that any plant material may beprocessed by the present invention and any plant oils may be targeted asthe oils to be extracted.

As the plant material is introduced to the primary entrainment section6, the plant material becomes entrained in the heated primary gas stream1. The entrained plant material travels with the primary gas stream intoone or more volatilization chambers 7 placed in series or in parallel.The primary entrainment zone and the volatilization chamber/chambers maytogether define an extraction chamber and, in some embodiments, may beintegrated with one another. Several methods may be used to achievevolatilization of the plant materials within the volatilization chamber,and this invention is not limited to any specific method ofvolatilization. A preferred way to volatilize the plant materials may beto use a form of pneumatic flash drying, however, adaptations of spraydrying, spin drying, pneumatic ring drying, spin dryers with agitators,dryers with classifiers, dryers with agitators, bed drying, any of thevolatilization methods proposed in the figures or text of thisdisclosure or any other method suitable to volatilize the plantmaterials may be used. Each of these methods will be known to those whoare skilled in the art of drying food products, pharmaceutical productsand industrial materials, however, the way that this invention is usingthese methods is unique. A detailed view of several embodiments of thevolatilization chamber 7 is illustrated in FIGS. 3, 4, 5, 6, 7, 8 a and8 b, and will be discussed in greater detail in the following sectionsof this disclosure.

Inside of some versions of the volatilization chamber 7, the plantmaterial is agitated and circulated while being exposed to the heatedprimary gas stream to cause rapid volatilization of particular plantoils that volatilize near, at or below the temperature maintained withinthe volatilization chamber by the primary gas stream. In otherembodiments, the plant material is forced into contact with a heatedsurface within the volatilization chamber. The temperature of the gasstream exiting the heater 2 may be adjusted to maintain a desiredtemperature in the volatilization chamber/s and to counteract anytemperature losses as the gas stream travels from the heater 2 to thevolatilization chamber/s 7. As will be discussed in detail in othersections of this disclosure, in some embodiments it is also possible todirectly heat the volatilization chamber. In most embodiments, targetinga specific temperature within the volatilization chamber will volatilizeplant oil compounds that volatilize near or below such a temperature. Inorder to isolate separate oil compounds, a method of successivelyprocessing the plant material at increasing temperatures over multipleextraction cycles may be used to fractionally isolate specific oils orspecific groups of oils. Alternatively, a sufficiently high temperaturemay be selected to volatilize a range of targeted plant oils in a singleextraction cycle. Such methods will be well understood by those of skillin the art. In some applications, it may be preferable to exclude adedicated volatilization chamber from the system if a sufficientvolatilization function can be obtained in the primary plant materialseparator 8. This is discussed in greater detail in a following section.

When cannabis is selected as the plant material to be processed, thepreferred oils to be volatilized may include the various chemical formsof cannabidiol (“CBD”), cannabidivarin (“CBDV”),delta-9-tetrahydrocannabinol (“THC”), delta-8-tetrahydrocannabinol,tetrahydrocannabivarin (“THCV”), cannabinol (“CBN”), cannabigerol,cannabichromene, chemically converted cannabinoids or any othercannabinoid. Other valuable terpenoid oils that may be extracted fromcannabis may include the various chemical forms of linalool,caryophyllene, myrcene, limonene, humulene, pinene. By manipulating thetemperature of the gas stream and/or heated surfaces that contact theplant materials within the volatilization chamber and completingsuccessive extraction cycles, it is possible to isolate the variousplant oils into substantially purified fractions. Alternatively, it ispossible utilize a wider temperature band within the volatilizationchamber to extract a range of plant oils in a single extraction cycle.As non-limiting examples, the following volatilization chambertemperatures may be utilized to extract various types of oils fromcannabis: To target the extraction of delta-9-tetrahydrocannabinol, thetemperature within the volatilization chamber should be kept near 315degrees Fahrenheit. To target a mostly purified form of cannabidiol, thetemperature should be kept near 315 degrees Fahrenheit in the firstextraction cycle to first remove the delta-9-tetrahydrocannabinol fromthe plant material, and then the plant material should be processed asecond time at a temperature near 356 degrees Fahrenheit to remove theremaining cannabidiol. To target extraction of bothdelta-9-tetrahydrocannabinol and cannabidiol in a single extractioncycle, the temperature within the volatilization chamber should be keptnear 356 degrees Fahrenheit to volatilize bothdelta-9-tetrahydrocannabinol and cannabidiol in the same cycle. Totarget extraction of tetrahydrocannabivarin and all cannabinoids with avolatilization temperature below that of tetrahydrocannabivarin, thetemperature of the volatilization chamber should be kept near 428degrees Fahrenheit. Other combinations of different temperatures orsuccessive extraction cycles may be used to target other oil compounds.Further discussion of temperatures and temperature ranges can be foundin following sections of this disclosure.

After circulating within the volatilization chamber 7, the processedplant material and the volatilized plant oils may travel with theprimary gas stream into a primary plant material separator 8. The oilmay be referred to as an extracted oil. A detailed view of an embodimentof the primary plant material separator 8 is illustrated in FIG. 9 andwill be discussed in greater detail in a following section of thisdisclosure. The processed plant material separator 8 is preferably acyclone or centrifugal separator, however other centrifugal ornon-centrifugal separation methods may be used to achieve the same orsimilar results. The primary plant material separator 8 separates theprocessed plant material from the primary gas stream containing thevolatilized plant oils. The separated plant material exits through thebottom of the primary plant material separator, while the primary gasstream, along with the volatilized oils, exits through the top of theprimary separator substantially free of entrained plant material. Itshould be noted that the positioning of the separated plant materialexits and primary gas stream exits may be flipped or vary in placementdepending on the differing requirements of the primary plant materialseparator design. Altering the placement of the exits should not beinterpreted as being outside the scope of this invention.

The separated processed plant material exiting the primary plantmaterial separator 8 may optionally become entrained in a secondary gasstream 25 in a secondary entrainment zone 27, or may simply be incommunication with a collection bin 29. The secondary gas stream 25 ispropelled by a secondary gas stream mover 26, which is preferably acentrifugal blower. However, any other method of propelling thesecondary gas stream may be used. The secondary gas stream is preferablykept at a lower temperature than the volatilization temperature of theplant oils in order to cool the processed plant material and prevent anycontinued volatilization or scorching from occurring. The processedplant material travels with the secondary gas stream into a secondaryplant material separator 28. The secondary separator 28, which ispreferably but not limited to a cyclone or centrifugal separator,separates the processed plant material from the secondary gas stream.However, any method capable of separating some or all of the processedplant material may be used. The processed plant material exits throughthe bottom of the secondary separator and is collected in a processedplant material collection bin 29. The secondary gas stream exits throughthe top of the secondary separator 28 substantially free of entrainedplant material and continues to recirculate through the secondary gasstream loop 25. Other forms of plant material separation and collectionmay be used, such as the methods commonly employed in shop vacuumcleaners. Alternatively, a simple method of allowing the processed plantmaterial to drop as a result of gravity or be mechanically propelledwith an auger screw or other mechanical device from the bottom of theprimary plant material separator 8 into a bin or disposal area may beused to avoid the need for a secondary gas stream 25 and the partsrequired for a secondary gas stream system. If such an alternative isused, it may be preferable in some applications to provide an airlockvalve, flapper valve or other method of isolating the primary plantmaterial separator from the outside atmosphere. One possible method ofplacing the primary plant material separator 8 is illustrated in FIG. 2,however, other methods may also be used.

The primary gas stream 1 and volatilized oils that exit the top of theprimary separator 8 may optionally pass through a gas stream filter 49.The gas stream filter 49 is preferably designed to remove any or most ofthe remaining fine particulates from the gas stream that are notcaptured by the primary plant material separator. The gas stream filter49 is preferably constructed of suitable materials to withstand thetemperature of the heated gas stream. Such materials may include, butare not limited to, fiberglass filters or strainers, stainless steel ormetal filters or strainers, sintered metal or glass filters, ceramicfilters, or filters constructed of any other suitable materials.

After exiting the gas stream filter 49, the primary gas stream 1 andentrained volatilized oils travel into a cooling chamber 9, which maytake the form of a cooling spray section 9, as shown. In embodimentsthat do not include a gas stream filter 49, the primary gas stream andentrained volatilized oils may travel into the cooling spray section 9after exiting the primary plant material separator 8. Inside the coolingspray section 9, the primary gas stream 1 and entrained volatilized oilsare contacted with a cooling spray 10 of a collection solvent that isemitted from one or more sprayers. The cooling spray 10 is supplied by aprimary pump 12 that moves collection solvent to various sprayers andother areas throughout the system. As illustrated in FIG. 1, the primarypump 13 draws collection solvent from the sump area 13, however, inother embodiments, the primary pump 12 may draw collection solvent fromother areas or other solvent reservoirs. In some embodiments, it ispreferred that the cooling spray instead be supplied by a dedicated pumpthat draws from a reservoir or other source of substantially purifiedcollection solvent. An example of such an embodiment is illustrated inFIG. 2 and a further description of such an embodiment is included inthe sections of this disclosure that discuss the evaporation device 31.

The collection solvent may be optionally cooled by a collection solventcooler 11. The collection solvent cooler 11 may be placed within thesystem such that it only cools the collection solvent before reachingthe cooling spray section 9 or it may be placed before or after theprimary pump 12 such that collection solvent spray traveling to anyparts of the system are cooled. The collection solvent cooler 11 ispreferably designed as liquid-cooled tube-in-shell heat exchanger orplate heat exchanger, however, air-cooled designs or any other suitableheat exchange device may be utilized. The collection solvent cooler 11may be cooled by any type of fluid or gas. The cooling supply may be aliquid or gas that is pumped through an air-cooled or liquid-cooled heatexchange device, a municipal water supply or any other suitable method.It should be noted that, in some embodiments, providing sufficientcooling to the collection solvent system can provide cooling andtemperature regulation of the entire system, in addition to that whichis required to provide cooling to the cooling section 9. A furtherdiscussion of potential heat exchanger designs can be found in thesections of this document describing the gas stream cooler 50 andevaporation device 31 condenser. The designs and cooling methods usedfor the collection solvent cooler 11, gas stream cooler 50, the solventrecovery device 22 and evaporation device 31 condenser may be usedinterchangeably as needed for each cooler or condenser device tofunction as required in different embodiments and applications.

Upon being contacted with the cooling spray 10 within the cooling spraysection 9, the primary gas stream is cooled and the volatized oilswithin the primary gas stream begins to condense. Preferably, the systemand the flow rates of the gas stream and cooling spray solvent aredesigned such that a large portion of the volatilized oils condensedirectly on the surface of the cooling spray droplets, where they becomedirectly captured in the collection solvent and drain directly orthrough other components of the system to reach the sump area 13 of thesystem. Much or all of the oils that do not condense on the droplets,condense within the gas stream into a fog of small and microscopic oildroplets, which travel out of the cooling section 9 entrained in theprimary gas stream 1. While it is preferred to use a cooling spray 10 asa gas stream cooling and oil vapor condensation method, other methodsmay be used, including but not limited to contacting the primary gasstream with cooling coils, passing the primary gas stream through atube-in-shell heat exchanger, or introducing a cooling gas directly intothe primary gas stream. As such, element 10 may represent any of thesecomponents or more than one such component.

Upon exiting the cooling spray section 9, the primary gas stream mayoptionally pass through a gas stream cooler 50. The gas stream cooler 50cools the gas stream, the entrained oil droplets and the mixture ofcollection solvent and captured plant oils preferably to a temperaturethat is sufficient to prevent heat degradation of the plant oils. Thegas stream cooler 50 is preferably designed as a tube-in-shell heatexchanger that uses a flow of liquid or gas as a coolant medium.However, any air or liquid-cooled device may be used, including but notlimited to exposing the gas stream to contact with vapor compression orabsorption chiller coils. For liquid cooled designs, any coolant may beused, including but not limited to municipal water, water or varioustypes of coolant fluids pumped or moved with the aid of a pump, vaporcompression or absorption chiller coils or any other suitable method.The liquid coolant may be cooled using forced air, passive air, a vaporcompression or absorption chiller, heat exchange with another liquid orany other suitable method. For air-cooled gas stream cooler designs, thegas stream cooler 50 may be cooled with forced air that is moved by theaid of an air mover, cool air from a vapor compression or absorptionchiller, evaporative cooling from a swamp cooler or similar device or bypassive contact with the surrounding atmosphere. It should be noted thatproviding sufficient cooling to the gas stream cooler 50 can providecooling and temperature regulation of the entire system. It is preferredthat the gas stream cooler be placed directly after a cooling spray 10or collection solvent spray section such that the collection solventwashes any condensed oils from the gas stream cooler 50 and such thatthe time that the collection solvent and plant oils are exposed to heatis minimized, however, other placements may be used.

After exiting the optional gas stream cooler 50, the primary gas streamcontaining a fog of any entrained oil droplets that were not previouslycaptured by the cooling spray, enters a sump section/liquid separator13. In embodiments that do not include a gas stream cooler 50, theprimary gas stream and entrained oil droplets may enter the sump section13 after exiting the cooling spray section 9. The sump section 13separates the majority of the liquefied collection solvent and extractedplant oil mixture from the primary gas stream and serves as a holdingarea for the collection solvent and captured extracted plant oil. Insome applications, it may be desirable to incorporate a separate liquidseparator (not shown) before the sump section 13 to facilitateseparation of the collection solvent from the primary gas stream. Such aseparate liquid separator could be as simple as a tee or bend in the gasstream path or may include demisting pads or other more advanced methodsof separation. In some embodiments, a separate collection solventreservoir (not shown) containing substantially purified collectionsolvent may also be included as a method to replenish any collectionsolvent that is lost or removed from the system as it operates.

After passing through the sump area 13, the primary gas stream and thefog of entrained oil droplets optionally enter an agglomeration section14. The diameter of the agglomeration section 14 is preferably largerthan that of the other passages within the primary gas stream loop 1 oris otherwise designed to be large enough to lower the velocity of theprimary gas stream and maximize the time that the primary gas stream andthe fog of oil droplets remain within the agglomeration section 14. Itis also possible to use a longer agglomeration section, adjust the gasstream velocity, or use multiple agglomeration sections in parallel orin series to attain a similar result of maximizing the time that the oildroplets spend in the agglomeration section. Within the agglomerationsection, the gas stream and fog of oil droplets are contacted withcollection solvent vapor provided by collection solvent injectors 15.The collection solvent vapor 15 condenses on the surface of the cooleroil droplets, causing them to grow larger and increase in size and mass.Increasing the size and mass of the entrained oil droplets greatlyenhances their removal from the gas stream in subsequent sections of thesystem. The preferred source of the collection solvent vapor is from thedistilled collection solvent outlet of the evaporation device 31,however, other methods of providing collection solvent vapor may beused. Alternatively, mixing a cooler gas stream with a warmer gas streamas it enters the agglomeration section will achieve a similar result.Such an alternative method is described in PCT/IB2014/002383. Anycollection solvent and other liquids that condense or coalesce on thesurfaces within the agglomeration section 14 eventually drain down theagglomerator walls and into the sump area 13 of the system. Preferably,the diameter of the entrance of the agglomeration section and thepassages leading from the sump area 13 to the agglomeration section 14should be designed to be large enough to reduce the velocity of theprimary gas stream such that condensing liquids can easily drain againstthe flow of the primary gas stream to reach the sump area 13. However,this may not be a requirement in some applications or with certainpositionings of the agglomeration chamber within the system, such aswhen the gas stream enters through the top of the agglomeration sectionand exits through the bottom, for example.

After exiting the optional agglomeration section 14, the primary gasstream 1 and mist of enlarged oil droplets enter a collection chambersection 16. In embodiments that do not include an agglomeration section,the primary gas stream and entrained oil droplets may enter thecollection chamber section 16 after leaving the sump section 13. In thecollection chamber 16, the oil droplets entrained in the primary gasstream are bombarded with a high pressure spray 17 of collection solventdroplets emitted from one or more collection solvent sprayers 17. Anyoil droplets that are impacted with collection solvent droplets 17 areeffectively captured in the collection solvent, which collides with thewalls of the collection chamber 16 and eventually drains to the sumparea 13. Upon exiting the collection chamber, most of the larger oildroplets have been removed from the primary gas stream, although some ofthe smallest oil droplets may still remain. It should be noted that insome embodiments that do not include a dedicated cooling section orcooling spray section 9 or a dedicated collection chamber 16, thecollection chamber section 16 could be considered to be the coolingsection 9 and the cooling 9 section could be considered to be thecollection chamber 16 section. In other words, the function of both thecooling spray section and the collection chamber section could becombined into one section in some embodiments of the system. In suchembodiments where these sections are combined, it is preferred that thecombined cooling spray/collection chamber section be located directlyafter the primary plant material separator 8 or directly after the gasstream filter 49, and in front of the gas stream cooler 50. However,other arrangements may be used. It should also be noted that in someembodiments the cooling section may be considered to be the gas streamcooler 50 or another cooling device or cooling area.

The primary gas stream optionally travels onward through a secondaryliquid separation section 18. The secondary liquid separation section 18separates the majority of the collection solvent from the primary gasstream to prevent the primary gas stream mover 19 from being overwhelmedby collection solvent. The secondary liquid separation section 18 may beas simple as a tee or bend in the gas stream passage or may include moreadvanced separation methods. The separated collection solvent drainsfrom the liquid separation section 18 and back into the sump section 13of the system. In some embodiments, the liquid separation section 18 maynot be needed, depending on the ability of the primary gas stream mover19 to handle entrained liquids. In other embodiments, it may bedesirable to intentionally introduce some liquid into the gas streammover 19 to facilitate cleaning and/or cooling of the gas stream mover19.

The primary gas stream exiting the liquid separation section 18 entersthe primary gas stream mover 19. In embodiments that do not include aliquid separation section 18, the primary gas stream enters the primarygas stream mover 19 after leaving the collection chamber 16. The primarygas stream mover 19 is preferably a regenerative blower, turbo blower,pressure blower or another type of blower that subjects the gas streamto a high level of centrifugal force, however, any method of propellingthe primary gas stream may be used. Upon entering the primary gas streammover 19, the primary gas stream is subjected to high centrifugalforces. Much or all of the remaining small and microscopic oil dropletsand collection spray mist droplets that were not captured in precedingsections of the system impinge with the blades and housing of theprimary gas stream mover 19. The oil and collection solvent dropletsthat impinge with the blades and housing of the gas stream mover 19 areeffectively captured and removed from the primary gas stream. Thecaptured oil and collection solvent drains from the exit of the primarygas stream mover or from a liquid drain port (not shown) within the gasstream mover, eventually reaching the sump section 13 of the system. Insome embodiments, the gas stream mover may be utilized as the primarymethod of separating the entrained plant oil droplets from the gasstream. In such embodiments, it is preferable that the gas stream moverbe supplied with a spray or stream of collection solvent to facilitatein washing the captured plant oils from the blower blades and housing.In such an embodiment, the gas stream mover or gas moving device may beconsidered part of the collection chamber and/or the gas moving devicemay form the only collection chamber for certain versions. Thearrangement of the gas stream mover within the system may also bealtered depending on the embodiment and application.

In some embodiments, the primary gas stream exiting the primary gasstream mover 19 travels into an optional droplet separator 20. Thisdroplet separator 20 is preferably a cyclone or centrifugal separator,although other methods may be used. The droplet separator separates muchor all of the remaining liquid droplets from the primary gas stream. Theseparated collection solvent and oil drains from the separator 20 intothe sump area 13 of the system.

To prevent a portion of the primary gas stream from bypassing the maingas stream loop and traveling through the drainage tube of the optionaldroplet separator 20, and to otherwise prevent a pressure differentialin the system from affecting drainage, an optional positivedisplacement/airlock pump 33 or similar device may be used to facilitatethe drainage of the droplet separator 20 to the sump section 13 of thesystem. Such an airlock/pump 33 or similar device may also be used inembodiments that do not include an optional droplet separator 20 tofacilitate drainage directly from the primary gas stream mover 19. Anairlock/pump 33 or similar device may also be used for a similarfunction in embodiments that include the optional demister/polishingsection 21 described in the following paragraph.

After exiting the droplet separator 20, the primary gas streamoptionally enters a demister/polishing section 21. In embodiments thatdo not include a droplet separator 20, the primary gas stream may enterthe demister/polishing section 21 after exiting the gas stream mover 19.The polishing section 21 polishes the primary gas stream and serves as afinal droplet separation stage to remove much or all of the remainingcollection solvent droplets prior to the primary gas stream passingthrough the primary gas heater. Providing effective droplet separationin the polishing section 21 and/or any preceding droplet separationsections prevents any droplets containing plant oils from coming incontact with the heated sections of the primary gas stream heater 2,thus preventing plant oils from burning, fouling or breaking down on thehot heater surfaces.

When the system is initially heated, the gases within the system willexpand and may attempt to exit the system through any poorly sealedareas. Likewise, when the system is cooling, the gases within the systemwill contract. In order to prevent pressure or vacuum from building inthe system, some embodiments provide a method of connecting the closedportion of the system to the atmosphere. Connection to the atmosphere isestablished through a solvent recovery device 22 such that as gases passout of the system, any evaporated collection solvent is condensed andreturned to the system. The solvent recovery device 22 is preferred toprevent collection solvent or volatilized plant oils from entering thesurrounding atmosphere. The solvent recovery device 22 may utilize anyknown method of solvent recovery, including but not limited to a coldtrap, a condensation tube, a filter, a distillation column, acommercially available solvent recovery system or any other suitablemethod. The solvent recovery device 22 may also contain a carbon filteror other type of odor capturing filter to prevent odors from escapingthe system. Various condenser designs may be employed as the solventrecovery device 22, including any of the condenser designs discussedbelow in the paragraphs describing the evaporation device condenser 55.

An optional out-only check valve 23 is attached to the exit end of thesolvent recovery device 22 to allow expanding gases to escape from thesystem when the system is heating and to prevent any atmospheric gasesfrom traveling backwards into the system through the solvent recoverydevice 22 when the system is cooling. To allow atmospheric gases toenter the system when the system is cooling, an in-only check valve 30may be connected to the processed plant material collection bin 29 orother places within the system.

Since the processed plant material will be removed from the system viathe collection bin 29, it is desirable in some embodiments thatcollection solvent vapors be evacuated from this portion of the systemto prevent their escape into the surrounding atmosphere. To keep thisarea evacuated of solvent vapors during times that the system is notcooling and thus naturally drawing gases in from the atmosphere, anevacuation pump 24 may be attached to the exit of the solvent recoverydevice 22. By continuously drawing a small amount of gas through thesolvent recovery device 22 at all times, a small amount of vacuum isgenerated in the system, which draws fresh atmospheric gases into theprocessed plant material collection bin 29 via the in-only check valve30, therefore displacing collection solvent vapors from the bin. Anadditional benefit of using an evacuation pump 24 in this manner is thatthe potential for solvent vapors escaping through any leaky seals withinthe system is mitigated. As an alternative to the evacuation pump, adisplacing gas may be introduced to the processed plant material bin orany other areas within the system that are deemed desirable to displace.A preferred displacing gas would be CO₂ or nitrogen, however, otherdisplacing gases may be used. It should be known that utilizing anevacuation pump 24 or displacing gas is beneficial for multiple purposes(including preventing the condensation of volatilized oils at the plantmaterial exit of the primary plant material separation device 8) andsuch use is not in any way dependent on a need to evacuate the processedplant material collection bin 29.

As will be discussed in a following section of this disclosure ingreater detail when describing the primary plant material separator 8and secondary plant material entrainment section 27 illustrated in FIG.9, the evacuation pump 24 and/or addition of a displacing gas creates aslight backflow through the plant material separator 8 and serves animportant function to prevent volatilized plant oils from escaping fromthe separated plant material exit 44 of the primary plant materialseparator 8 and condensing on the separated plant material exit 44 ofthe primary plant material separator 8 and/or the parts within thesecondary gas flow loop 25 and/or processed plant material bin 29. Ifplant oils condense in these areas, it could cause plant material tostick to the internal surfaces of these parts and block the flow ofseparated plant material to the collection bin 29. While a passivemethod of evacuating plant oil vapors from these areas to preventcondensation is preferred, in some embodiments, it may be beneficial toinclude an auger screw or mechanical scraping method to ensure thatthese parts never become clogged.

In order to separate the captured plant oils from the collection solventand plant oil mixture, some versions of the invention may optionallyinclude an oil/solvent separation system such as an evaporation device31. The evaporation device 31 is preferably, but not limited to, anevaporation device such as a thin film evaporator, wiped filmevaporator, short path evaporator, rising film evaporator, falling filmevaporator, spray dryer evaporator, centrifugal thin-film evaporator, ora conventional still design such as, but not limited to, stills that arecommonly used to distill ethanol-based spirits. However, any suitableevaporation device may be used and one or more evaporation devices maybe used alone or in combination for enhanced evaporation or multipleeffect evaporation. Non-evaporative oil separation devices mayalternatively be utilized. The evaporation device 31 may be operated atatmospheric pressure, under vacuum or above atmospheric pressure. Heatmay be supplied to the evaporation device using electric heatingelements, steam from a steam generator, a hot oil system, a thermalfluid, a heated gas or any other suitable method of supplying heat. Inthe case that the evaporation device is a thin film or wiped filmevaporator, it is preferred that heat be supplied to the evaporator bywrapping the evaporation section with heat cables or by including asteam jacket or thermal fluid jacket around the evaporation section ofthe device and providing heat with a steam generator or thermal fluidsystem. In the case that the evaporation device is a rising film orfalling film evaporator, it is preferred that heat be supplied to thefalling or rising film section by a steam generator or thermal fluidsystem.

As the system is running, or in some embodiments, after the system hascompleted an extraction cycle, the evaporation device 31 draws aportioned flow of the mixture of collection solvent and captured plantoils from the sump area of the system by diverting some of thepressurized solvent from the primary pump 12 with the aid of aproportional valve, solenoid valve or other suitable diversion and/orportioning method (not shown) or with the aid of a dedicated feed pump60 (shown in FIG. 2). Upon entering the evaporation device 31, thecollection solvent is evaporated and distilled from the solvent andplant oil mixture and the solvent is reintroduced to the system as asubstantially purified collection solvent. In the embodiment illustratedin FIG. 1, the purified collection solvent is reintroduced to the systemas a vapor via collection solvent vapor injectors 15 in theagglomeration section 14 of the system. In this manner, the evaporatedcollection solvent vapors may be used to facilitate the function of theagglomeration section 14. The purified collection solvent mayadditionally or alternatively be introduced as a vapor to other sectionsof the system to aid in cleaning of the various components or serveother functions as required.

When the mixture of collection solvent and captured plant oils areintroduced to the evaporation device, the plant oils, which preferablyhave a higher boiling point than the collection solvent utilized, do notreadily evaporate within the evaporation device 31 and are concentratedinto a substantially pure form as the collection solvent is distilledaway. The concentrated plant oils exit the evaporation device 31 as asubstantially pure extract which is subsequently collected in an extractcollection area 32 as a final product of the system. Additionaldiscussion of evaporation methods can be found in PCT/IB2014/002383,however, these methods should not be viewed as limiting. As analternative to an evaporation device, other methods of separating theplant oils from the collection solvent may be used. In embodiments thatuse collection solvents that are immiscible with the plant oils beingcollected, stratification methods of separation may be employed.Chromatography methods may also be used to separate the oils from thecollection solvent. Such methods serve as examples and are not limiting.Those of skill in the art will be able to determine the best separationmethod for different applications of the current invention.

FIG. 2 illustrates an additional embodiment of the present invention. InFIG. 2, the substantially purified collection solvent vapor exiting theevaporation device 31 passes through a condenser 55 to condense thecollection solvent vapor into a liquid. The liquefied collection solventexiting the condenser 55 flows into a purified solvent reservoir 56. Adedicated collection solvent pump 57 draws the substantially purifiedcollection solvent from the purified solvent reservoir 56 and sprays thepurified collection solvent directly into the cooling spray section 9via the cooling spray 10. Alternatively, the purified solvent may bepumped directly from the condenser 55. Arranging the system in a mannerwhereby only substantially pure collection solvent is used in thecooling spray section 9, rather than recirculating collection solventfrom the sump area 13, ensures that previously captured plant oils arenot exposed to further heat by contacting the heated gas stream prior toit being cooled. In other applications and embodiments, it may bedesirable to reintroduce the condensed collection solvent directly tothe sump area 13 or any other area of the system where it is needed.

In embodiments of the invention where the evaporation device 31 includesa condenser 55, any condenser design may be used, including but notlimited to liquid-cooled designs such as a Liebig, Allihn, Graham,Dimroth, Friedrichs or tube-in-shell condenser, or air cooled designssuch as spiraled tubes, radiator style condensers or other designs thatwill be readily known to those of skill in the art. For liquid-cooledcondenser designs, any coolant may be used, including but not limited tomunicipal water, water or various types of coolant fluids pumped ormoved with the aid of a pump, vapor compression or absorption chillercoils or any other suitable method. The liquid coolant may be cooledusing forced air, passive air, a vapor compression or absorptionchiller, heat exchange with another liquid or any other suitable method.For air-cooled condenser designs, the condenser may be cooled withforced air that is moved by the aid of an air mover or by passivecontact with the surrounding atmosphere. Such condenser designs andcooling methods may also be employed in the solvent recovery device 22,as mentioned above.

It is highly desirable to keep the internal surface temperatures of allportions of the system that contact the gas stream between the gasstream heater 2 and the first areas exposed to collection solvent oranother cooling method near or above the condensation temperature of thevolatilized plant oils. This is beneficial to prevent condensation ofvolatilized oils on undesired surfaces within the heated portions of thesystem, which could potentially damage the oils and/or hinder theirrecovery from the system. In order to maintain the temperature of thegas stream and to prevent condensation of volatilized oils on undesiredsurfaces within the heated portions of the system, in many embodimentsof the invention it will be advantageous to house all or most of theheated portions of the system, including but not limited to all, some orany combination of the gas stream heater 2, the primary plant materialseparator 8, the primary plant material separator lower exit 44(discussed in further detail in a following section), the optional gasstream filter 49 and the volatilization chamber/s 7, together in onepassively insulated or actively heated box or heated chamber to simplifythe insulating or heating of such components. Such a heated chamber maybe passively insulated with a thermal insulation barrier such asfiberglass, ceramic wool, silica insulation, calcium silicate, aerogel,ceramic insulation, rock wool, mineral wool or any other suitableinsulating medium. If the heated chamber is actively heated, electricelements may be used within the open space of the oven cavity with orwithout the aid of a convection fan, or a heated gas may be pumpedthrough the oven chamber. Alternatively, the heated parts may be housedtogether in a vacuum chamber of suitable size for passive insulation, ora steam chamber of suitable size that may be supplied with steam as aheat source for active heating. The heated parts may also be wrappedwith a heating cable. Finally, the heated parts may be contained in achamber with a thermal heating liquid. Any heating or insulating methodknown to those of skill in the art may be utilized and still fall withinthe scope of this invention. It should be known that in most embodimentsit may be important to construct the gas stream path such that thehopper section 4 is not housed within the oven chamber, yet is able toprovide plant material to the entrainment zone 6. In embodiments whereinthe heated components of the system are not contained within a heatedbox/oven chamber, or in embodiments wherein additional heating orinsulation of the heated components is required, the heated componentsmay be individually insulated or actively heated as discussed in thefollowing sections of this document.

In some embodiments, a method of cooling the overall system must be usedto prevent the system from overheating. Various methods of cooling theoverall system using the collection solvent cooler 11 and/or the gasstream cooler 50 have been discussed in this disclosure. Additionalmethods, such as, but not limited to, circulating forced air or acooling fluid over the external parts of the system may also be used.Passive methods of cooling the system, such as, but not limited to,including cooling fins or protrusions on various components of thesystem and gas stream loop may also be employed. It is also possible tohouse the system in a room or chamber of a regulated temperature.Further discussion of various additional cooling methods can be found inPCT/IB2014/002383.

Since the gas stream in most embodiments of the present invention willbe saturated with collection solvent vapors in some areas, it ispossible to promote an environment in the cool sections of the systemthat causes collection solvent vapors to condense on the internalsurfaces of these sections. By causing collection solvent to condense onthe internal surfaces of the cool sections of the system, the condensingcollection solvent can be used to aid in washing these surfaces of anyaccumulated plant oils. To promote such a “condensation washing”environment, it is desirable to always keep the gas stream warmer thanthe internal surfaces of any areas of the system that contact the gasstream after the first cooled section of the system and before the gasstream heater section. Exceptions to this are the hopper section, thesecondary gas stream 25 sections and separated plant material bin 29,where it is not desirable to have condensing collection solvent. Thesolvent that condenses on the internal surfaces of the cool sections ofthe system, along with any accumulated oils, drain through the system toeventually be collected in the sump area 13. Additional methods of“condensation washing” are described in PCT/IB2014/002383. Other methodsmay also be used.

The various valves, pumps, airlocks, electrical heaters and/or steamheaters, and any other controllable components of the system describedin this disclosure may be regulated or controlled by mechanical methodsand/or electronic temperature and/or pressure switches. It is, however,preferred that the temperatures and pressures within the system, theoptional steam generator, evaporation device and various pumps, valves,airlocks, gas movers and other controllable components within the systembe controlled by one or more programmable logic controllers (PLCcontrol) and/or proportional integral derivative controllers (PIDcontrol) and/or other forms of computerized controls. Utilization ofsuch electronic devices may achieve more precise control of thetemperatures, pressures and various actions of the system. Whenelectronic controls are implemented, the temperatures may be monitoredby thermocouples, resistance temperature detectors (RTD sensors) and/orother temperature detection methods, the pressures may be monitored byelectronic pressure sensors and/or mechanical pressure devices and/orother detection methods, the gas flow and liquid flow may be detected byelectronic mass flow meters, pressure sensors, pressure differentialsensors, Coriolis meters and/or other detection methods, the position ofcomponents may be detected with limit switches, position sensors,proximity sensors and/or other detection methods, the levels of fluidsmay be detected with optical, electrical, conductive, ultrasonic,capacitive, float switches and/or other detection methods and the levelsof dry materials may be detected with optical, electrical, conductive,ultrasonic, capacitive, float switches, rotary dry level detectorsand/or other detection methods. It may also be desirable to includesensors that can detect the saturation levels of water, plant oils orother liquids that have accumulated in the collection solvent mixture,such as capacitance sensors, conductivity sensors, specific gravitysensors, moisture sensors, refractometers or other types of sensors.Other sensors of various available designs may also be utilized asneeded to measure the state of the various components and still fallwithin the scope of this invention. Non-limiting examples of how suchthermocouples, sensors and devices that may be placed within the presentinvention can be found in PCT/IB2014/002383, which is incorporated inthis application in its entirety by reference, however, the placement ofsensors will be apparent to those who are skilled in the art. Thevarious temperature, pressure, flow rate and other sensors may be placedwithin any section of the system, in any quantity and in any order andstill fall within the scope of this invention. The various PLC, PID,computer or other control methods may regulate components within thesystem with various types of commercially available digital, analogand/or other types of input/output modules (TO modules), steppercontrollers, variable frequency controllers, solid state relays,conventional magnetic relays and/or any other suitable method.

FIG. 3 provides a detailed view of an embodiment of the volatilizationchamber section of the system. The purpose of the volatilization chamberis to expose the plant material entrained in the primary gas stream to aturbulent and/or agitated environment to maximize contact with the gasstream and facilitate rapid volatilization of the plant oils containedwithin the plant material. This disclosure describes multiple methods toattain these results, including omission of the volatilization chamberin favor of a primary plant material separator with heated walls,however, other methods may be used to attain similar results and stillfall within the scope of this invention. As illustrated in FIG. 3, theprimary gas stream carries the entrained plant material into thevolatilization chamber through an upward facing entry tube 34. Uponleaving the tip of the entry tube 34, which may include a high-velocitynozzle tip in some applications, the entrained plant material is blastedupward toward the top of the volatilization chamber 7. As the plantmaterial travels upward, it is exposed to a turbulent reversal of thegas stream flow within the volatilization chamber. This action causesforceful agitation of the plant material and maximizes its contact withthe heated primary gas stream to facilitate rapid volatilization of theplant oils contained within the plant material. The primary gas stream,along with the entrained plant material, exit the volatilization chamberthrough an exit passage 35 at the bottom of the chamber and travelonward to the primary plant material separator 8. One or morevolatilization chambers of this type may be used in series or inparallel or in combination with other types of volatilization chambers.As such, element 7 in FIG. 1 and FIG. 2 may represent one or morevolatilization chambers.

In order to maintain a sufficient temperature of the gas stream as itpasses through the volatilization chamber and to prevent condensation ofvolatilized oils on surfaces within the volatilization chamber, it ispreferred that most embodiments of the volatilization chamber discussedwithin this disclosure be contained or wrapped in a thermal insulationbarrier and/or be provided with an active heat source. Such a heatsource or thermal barrier may optionally be eliminated if thevolatilization chamber/s are housed together with all or some of theother heated sections of the system within an insulated or heatedchamber as discussed above. As a non-limiting example that may beapplied to any of the embodiments of the volatilization chamberdiscussed or referred to in this disclosure, in FIG. 3, thevolatilization chamber is illustrated housed within a heating jacket 36.To provide heat to the volatilization chamber 7, saturated steam of aspecific pressure and temperature, a heated gas of a specifictemperature or a heated thermal fluid of a specific temperature ispumped or otherwise introduced to the heating jacket through an entrypassage 37. The steam and/or condensed steam, heated gas or thermalfluid circulates out of the heating jacket through an exit passage 38.In embodiments where steam is used as the heating medium, it ispreferred, but not required, that the steam be supplied by the samesteam generator that provides heat to the primary gas heater 2.Alternatively, an electrical heat source within the jacket space or anelectrical heating wire wrapped directly around the volatilizationchamber may also be used. Any of these methods may be used to heat anyof the embodiments of the volatilization chamber discussed or otherwisereferred to in this disclosure.

In some embodiments, it may be preferred to passively insulate thevolatilization chamber with a thermal insulation barrier such asfiberglass, ceramic wool, silica insulation, calcium silicate, aerogel,ceramic insulation, rock wool, mineral wool or any other suitableinsulating medium. It may also be preferred in some applications tohouse the volatilization chamber within a vacuum jacket. As anon-limiting example, such a vacuum jacket may look substantiallysimilar to the heating jacket 36 illustrated in FIG. 3, except therewould be no entry 37 or exit passages 38 for a heating medium. Instead,of heating medium entry and exit passages, an evacuation passage wouldbe included that may include a check valve or similar vacuum containmentmethod. Alternatively, the vacuum jacket may be permanently sealed orwelded closed to retain the vacuum. Any of these methods may be used toinsulate any of the embodiments of the volatilization chambers discussedor otherwise referred to in this disclosure.

FIG. 4 illustrates an additional embodiment of the volatilizationchamber section 7 of the system that utilizes a modified spray dryingtechnique. Conventional industrial spray drying techniques typicallyinvolve spraying a mostly liquid feed that contains some solids into aheated gas stream as it enters a drying chamber. Those of skill in theart will be familiar with the design of such spray drying chambers.Within a conventional spray drying chamber, the liquids are evaporatedand subsequently vented as waste, while the solids are collected as thefinal product. (An example of a conventional spray drying applicationwhere the liquid is vented and the solids are collected as the finalproduct is the production of powdered milk.) In the current embodiment,the opposite final product is desired. Instead of the solids beingdesired, the liquid portion is desired as a final product. Therefore,the utilization of the spray drying technique is modified in thisinvention to handle a mostly dry feed instead of a mostly liquid feed.In the current invention, powdered or finely-ground plant material (asolid that contains liquid oils) is introduced into a heated gas streamthat enters a drying chamber/volatilization chamber. This heated gasstream is the primary gas stream as defined in this invention. Theprimary gas stream carries the entrained plant material into thevolatilization chamber 7 through a downward facing entry tube 39 with anozzle tip. The primary gas stream and plant material rapidly exitingthe nozzle facilitates a turbulent flow of the heated gas stream withinthe volatilization chamber and agitates the plant material to causerapid volatilization of the oils contained within the plant material.The primary gas stream and entrained plant material exit thevolatilization chamber through an exit passage 35 in the bottom of thechamber 7. One or more chambers of this type may be used in series or inparallel or in combination with any other types of volatilizationchambers. Utilization of different nozzle designs, the addition ofpressurized and/or hot air at the nozzle site, modifications to thedimensions and diameter of the spray drying chamber and other changesmay benefit volatilization of the plant material and/or prevent plantmaterial from sticking to the walls of the chamber in similar ways thatsuch modifications benefit conventional spray drying techniques. In someembodiments, it may be advantageous to introduce the plant materialdirectly at the nozzle site versus upstream of the nozzle in theentrainment area 6. Those of skill in the art will understand that manycommercial spray drying techniques and designs may be adapted for use inthe present invention. Such adaptations will still fall within the scopeof the present invention. As with other embodiments of thevolatilization chamber, in order to maintain the temperature of the gasstream and to prevent condensation of the volatilized oils on thesurfaces within the volatilization chamber, it is preferred that thevolatilization chamber be provided with its own heat source and/or athermal insulation barrier. Examples of such heat sources and thermalbarriers were discussed above, and may be applied to all embodiments ofthe vaporization chamber.

FIG. 5 illustrates a third embodiment of the volatilization chamber 7that is designed to centrifugally force the plant material into contactwith the heated walls of the volatilization chamber to induce rapidvolatilization of the plant oils. One or more chambers of this type maybe used in series or in parallel or in combination with other types ofvolatilization chambers. In the embodiment illustrated in FIG. 5, theprimary gas stream 1 and the entrained plant material enter thevolatilization chamber through a tangential entrance 40 at the upper endof the volatilization chamber 7. As the primary gas stream tangentiallyenters the volatilization chamber 7, the entrained plant materials arecentrifugally forced into contact with the outer walls 41 of thechamber, where they spiral around the walls 41 of the volatilizationchamber multiple times before eventually reaching the bottom exit 35 ofthe volatilization chamber. In order for successful volatilization ofthe plant oils to occur using this method, it is highly preferred thatthe walls 41 of the volatilization chamber be in contact with a heatsource. However, in some applications the use of a thermal barrier maysuffice. Examples of such heat sources and thermal barriers arediscussed above, and may be applied to this embodiment and all otherembodiments of the vaporization chamber.

FIG. 6 illustrates an embodiment of the volatilization chamber 7 thatutilizes a modified form of pneumatic flash drying to induce rapidvolatilization of oils within the plant material. One or more chambersof this type may be used in series or in parallel or in combination withother types of volatilization chambers. The primary gas streamcontaining entrained plant material enters the flash dryingvolatilization chamber 7 through a bottom entry passage 46 and carriesthe plant material upwards against gravity before exiting the chamberthrough an exit passage 47. The upper exit passage 47 may be relocatedto the side of the chamber, however, it is preferred that the lowerentry passage 46 remain at the lowermost point of the chamber 7. Thediameter of the flash drying chamber and the flow rate of the primarygas stream must be carefully designed such that the heated gas flowingthrough the chamber is moving slightly faster than the natural freefallvelocity of the plant material particles being processed. At this gasstream velocity, contact of the heated gas stream and plant particles ismaximized, causing rapid volatilization of the plant oils. The length ofthe flash drying volatilization chamber 7 may be adjusted to maximizevolatilization, or may be repeated with several shorter chambersarranged in series. As with other embodiments of the volatilizationchamber, in order to maintain the temperature of the gas stream and toprevent condensation of the volatilized oils on the surfaces within thevolatilization chamber, it is preferred that the volatilization chamberbe provided with its own heat source and/or a thermal insulationbarrier. Examples of such heat sources and thermal barriers arediscussed above, and may be applied to all embodiments of thevaporization chamber.

FIG. 7 illustrates an additional embodiment of the volatilizationchamber that is designed to prevent plant material that is still heavyladen with oils or has clumped into lumps from escaping thevolatilization chamber until it has been broken up into small particlesand has been fully stripped of its desirable oils. This special type ofvolatilization chamber is an adaptation of a flash drying chamber thatis designed such that the diameter of the chamber and the gas streamflow volume create a gas velocity that only allows the smallest and mostthoroughly oil-stripped particles of plant material, which are lightenough to float upward in the gas stream, to exit the top of thechamber. Larger lumps or oil laden plant particles, which are too heavyto be carried up and out of the chamber, remain tumbling in an agitationzone until they are broken up and evaporated of their oils. It is onlyafter the lumps of plant material are broken up and evaporated of theirdesirable oils that the plant materials become light enough and smallenough to exit the chamber. As illustrated in FIG. 7, the gas streamcarrying entrained plant material enters the volatilization chamberthrough a bottom passage 46. The diameter of the bottom passage isreduced to a small diameter before entering the chamber to form an airblade nozzle 47. The high velocity air from the nozzle 47 turbulentlyenters the volatilization chamber and helps forcefully break apart anylumps or chunks of plant material that are too heavy to travel upward inthe chamber. The lighter and smaller particles of plant material arequickly stripped of their desired oils and continue to travel upwardwith the gas stream to exit the chamber through an exit passage 48. Theheavier chunks of plant material cannot attain lift in the lowervelocity gas stream areas of the chamber and remain near the bottom ofthe chamber where they continue to tumble and impact one another and thewalls of the chamber while simultaneously getting dryer as the oils thatthey contain volatilize in the heated chamber at a slower rate.Together, this effect of tumbling and drying causes the plant materiallumps to break apart into progressively finer and finer particles. Oncethe particles are fine and light enough, they can attain the lift thatthey need to be carried by the rising gas stream to exit the top of thechamber through the exit passage 48. Other embodiments of this uniquevolatilization chamber design may include hollow or solid balls or beadsor other objects of other shapes constructed of stainless steel, othermetals, ceramics, thermal plastics, or any other suitable material toaid in breaking up the plant material. A non-limiting example of such anelement is represented by a ball 51 in FIG. 7. In such embodiments, theballs or other milling objects will be thrown around within the chamberby the air nozzle 83 to facilitate breaking up of the plant material. Anexcluder screen or other exclusion method may optionally be included toprevent a stray ball or milling object from escaping the volatilizationchamber. Alternatively, the fast moving gas stream entering the chambermay be used to power a turbine blade (not shown) to a high velocity. Theoptional high velocity turbine blade may be used to break up any largeparticles of plant material moving around the bottom sections of thechamber. Such a blade could also be rotated by an externally poweredshaft that passes through a wall of the chamber or incoming gas passage,or by a magnetic coupling to avoid the need for a shaft seal and/orshaft penetration hole that could potentially leak. The blade andmilling object designs used in this embodiment of the vaporizationchamber could be adapted for use in any of the vaporization chamberembodiments discussed in this disclosure. While the volatilizationchamber illustrated in FIG. 7 is illustrated as having a concave bottomarea, in other embodiments it may be desirable to utilize a conicalbottom area to continuously funnel the falling heavier plant materialsback into the air pick or blade area. As with other embodiments of thevolatilization chamber, in order to maintain the temperature of the gasstream and to prevent condensation of the volatilized oils on thesurfaces within the volatilization chamber, it is preferred that thevolatilization chamber be provided with its own heat source and/or athermal insulation barrier. Examples of such heat sources and thermalbarriers are discussed above, and may be applied to all embodiments ofthe vaporization chamber.

FIGS. 8a and 8b illustrate a cross-sectional and a top view of anotherembodiment of the volatilization chamber that is designed to preventplant material that is still heavy laden with oils or has clumped intolumps from escaping the volatilization chamber until it has been brokenup into small particles and been fully stripped of its desirable oils.In this embodiment, the gas stream and entrained plant material entersthe volatilization chamber through a tangential side entrance 70. Thegas stream enters at a high velocity and causes the entrained plantmaterials to spiral rapidly within the volatilization chamber.Optionally, hollow or solid balls or beads or other milling objects ofother shapes constructed of stainless steel, other metals, ceramics,thermal plastics, or any other suitable material may be included in thevolatilization chamber to aid in breaking up the plant material. Thesemilling objects are preferably sized such that they cannot exit thechamber and continue to rapidly spiral along the walls of the chamber,grinding and breaking up any large plant material particles. Optionally,an excluder screen or other exclusion device may be used to prevent anychance of the milling objects from exiting the chamber. A non-limitingexample of a few hollow milling balls 51 are illustrated in FIG. 8a .The exit of the volatilization chamber is designed and positioned suchto serve as a particle classifier that allows only the smallest andlightest particles of plant material to leave the chamber. In this way,only the plant materials that have been thoroughly broken up and havebeen substantially stripped of their desired oils can exit the chamber,where the heavier plant materials that still contain oils will continueto circulate within the volatilization chamber until they are lightenough to leave. The embodiment of the volatilization chamberillustrated in FIGS. 8a and 8b functions in a similar way to a cycloneseparator in that it centrifugally excludes larger particles fromleaving through the primary chamber exit 71. However, it is verydifferent from a typical cyclone separator in that it does not have asecondary exit for captured particles to escape and that eventually allof the plant material particles do escape through the primary exit.Instead of permanently separating the plant particles from the gasstream like a conventional cyclone, the plant material particlescontinue to circulate within the volatilization chamber until they arestripped of enough of their oils and are ground to a fine dust. When theplant material particles have attained a low enough mass to no longer beaffected by centrifugal separation, they are carried out the main exitby the gas stream and eventually are separated by the primary plantmaterial separator. By delaying the departure of the plant materialsfrom the volatilization chamber in such a way, nearly completeextraction of the plant oils may be attained. The embodiment of thevolatilization chamber illustrated in FIGS. 8a and 8b may be used inparallel or in series with additional similar volatilization chambers orin combination with any of the other volatilization chambers describedin this disclosure. In particular, it may be beneficial to use thisembodiment of the volatilization chamber before a flash drying chambersuch as the embodiment illustrated in FIG. 6.

While not illustrated in any figures in this disclosure, anotherembodiment of the volatilization chamber that may be preferred with sometypes of plant materials would consist of a pneumatic ring dryer design.The term pneumatic ring dryer is well defined in industrial dryingliterature and the design of a ring dryer will be well known to those ofskill in the art. A ring dryer version of the volatilization chamberwill have the benefit of allowing plant material to graduate through thesystem only after the desirable oils have been volatilized. Othermethods that may attain excellent volatilization of the plant oils mayinclude spin flash drying systems, spin flash drying systems withagitator blades, rotating drum dryers, ball mill dryers, dryers withparticle classifiers and other methods that will be known to those ofskill in the art.

FIG. 9 illustrates a detailed view of an embodiment of the primary plantmaterial separation device 8 and the secondary plant materialentrainment section 27. As illustrated in FIG. 9, the primary separationdevice is a cyclone separator. However, other centrifugal ornon-centrifugal separation methods may be used. The primary gas streamand entrained plant materials enter the primary plant materialseparation device through a tangential entrance 42 at the side of theseparator 8. Upon entering the primary plant material separator, theentrained plant materials are centrifugally forced into contact with theouter walls 43 of the separator 8, where they spiral down the walls 43of the separator and fall from the bottom exit of the separator andeventually reach the processed plant material collection bin 29. Theprimary gas flow exits through the top portion 53 of the separatorsubstantially free of entrained plant material and continues to theoptional gas stream filter 49 or directly to the cooling spray section 9of the system. While many centrifugal separators are oriented in theposition described in FIG. 7, it will be known to those of skill in theart that the orientation of the separator may be altered and that arepositioning of the top and/or bottom exits and/or side entry points(if applicable) will still fall under the scope of the presentinvention.

It should be noted that one or more primary plant material separationdevices may be used in parallel or in series or both in parallel and inseries to obtain more complete separation of the entrained plantmaterials from the primary gas stream. In the case that a cycloneseparator is used as the primary plant material separation device,better separation can be achieved by the utilization of several smallcyclones in parallel, each of a smaller diameter with a lower volume ofgas flow, versus using one cyclone of a large diameter with a highervolume of gas flow. Placing cyclones in series also achieves betterseparation. In the interest of maintaining simplicity in the design ofthe invention, it is preferable to use the least amount of cyclonesrequired to achieve the desired level of separation. This applies notonly to the primary separation cyclone, but also to any other plantmaterial or droplet separation cyclones used within the system.

As illustrated in the embodiment of the primary plant material separator8 that is depicted in FIG. 9, as the separated plant material falls fromthe bottom exit of the separator 8, it optionally passes through aspecialized, heated and/or insulated exit tube 44. This heated exit tube44 is also illustrated in the flow diagrams in FIG. 1. Upon reaching thebottom of the heated exit tube 44, the processed plant material fallsinto the secondary entrainment section 27 where it is entrained in thesecondary gas stream 25 and propelled into the secondary plant materialseparator 28 to eventually fall into the processed plant materialcollection bin 29. It is preferable that the secondary gas stream 25 bemaintained at a lower temperature than the primary gas stream 1, suchthat the processed plant material is cooled upon coming in contact withthe secondary gas stream 25. By cooling the processed plant material,further volatilization is arrested and heat degradation of the plantmaterial is prevented. This is especially important in the case that theoperator of the system desires to perform a second, higher temperatureextraction of the plant material to extract plant oils of a higherboiling point than those that were extracted in the first extractioncycle. Failure to cool the processed plant material could damage theremaining oils and could also lead to degraded oil vapors travelingupwards from the collection bin and into the primary gas stream as thesystem operates, thereby reducing the quality of the extract. As analternative, a simple method of allowing the processed plant material todrop as a result of gravity or be mechanically propelled from the bottomof the primary plant material separator 8 into a bin or disposal areamay be used to avoid the need for a secondary gas stream 25 and theparts required for a secondary gas stream system. If such an alternativeis used, it may be preferable in some applications to provide an airlockvalve, flapper valve or other method of isolating the primary plantmaterial separator from the outside atmosphere.

As processed plant material travels down the heated exit tube 44, aportioned, small volume of atmospheric gas or displacing gas issimultaneously entering the system through the in-only check valve 30connected to the processed plant material collection bin 29 andsubsequently mixing with the gases in the secondary gas stream 25. Thisgradual inward flow of the atmospheric or displacing gas slowly flows upinto the system through the same heated tube 44 that the processed plantmaterial is falling down, against the downward flow of falling plantmaterial. This flow of atmospheric gas or displacing gas (illustrated bythe small, upward traveling arrows 45 in the heated exit tube 44) servesan important purpose—it prevents plant oil vapors from escaping from theexit of the primary plant material separator 8 and condensing on theparts within the secondary gas flow loop 25 and processed plant materialbin 29. To prevent any condensation from occurring within the lower exitportion of the primary plant material separator 8, the heated exit tube44 should be of sufficient length such that the vapor-free atmosphericor displacing gas is heated to near or greater than the volatilizationtemperature of the plant oils being volatilized prior to reaching thebottom portion of the primary plant material separator 8. The heatsource for the heated exit tube 44 may be the heating jacket 36described in the following paragraph, or a separate heating jacket thatis heated by a similar method to the heating jacket 36 described in thefollowing paragraph. Alternatively, the heated exit tube 44 may bedirectly wrapped in an electric heating cable or similar device. Thedisplacing gas may also be heated by other methods. One non-limitingexample would be to place a spiraled atmospheric gas or displacing gastube constructed of a metal, silicone or other heat resistant materialin a heated area of the system or within the heated chamber that housessome or all of the heated components in some embodiments, such that thedisplacing gas is heated prior to being introduced to the separatedplant material exit tube 44. Another non-limiting example would be towrap a displacing gas or atmospheric displacing gas tube of suitablematerial in heating coils. Other methods may also be used to heat thegas being introduced to the separated plant material exit 44. In caseswhere the method of displacing volatilized plant oils from the separatedplant materials exit 44 are not effective or not deemed to be the bestoption, mechanical methods of removing accumulated plant oils from theplant material exit 44 and pathways to the separated plant material bin29 may be employed. A few non-limiting examples include utilization ofan auger screw or auger conveyor, rotating scraper blades, plungerpistons, a belt system or other methods that will be known to those ofskill in the art.

It should be noted that supplying the walls 43 of the primary plantmaterial separator 8 with a sufficient heat source may be desirable andmay have the added benefit of providing an option to omit the precedingvolatilization chamber section 7 of the system in some circumstances. Ifsufficient heat can be transferred to the plant material through directcontact with the heated walls 43 of the primary plant material separator8, sufficient volatilization and extraction will occur without the needfor a separate volatilization chamber 7. As illustrated in FIG. 9, boththe processed plant material exit tube 44 and the primary plant materialseparator 8 are housed within a heating jacket 36. To provide heat tothe plant material separator 8 and plant material exit tube 44,saturated steam of a specific pressure and temperature, a heated gas ofa specific temperature or a heated thermal fluid of a specifictemperature is pumped or otherwise introduced to the heating jacketthrough an entry passage 37. The steam and/or condensed steam, heatedgas or thermal fluid circulates out of the heating jacket through anexit passage 38. In embodiments where steam is used as the heatingmedium, it is preferred, but not required, that the steam be supplied bythe same steam generator that provides heat to the primary gas heater.Alternatively, an electrical heat source within the jacket space or anelectrical heating wire wrapped directly around the plant materialseparator 8 and/or exit tube may also be used.

As with the previously described volatilization chamber embodiments, insome embodiments of the primary plant material separator, it may bepreferred to passively insulate the primary plant material separator 8with a thermal insulation barrier such as fiberglass, ceramic wool,silica insulation, calcium silicate, aerogel, ceramic insulation, rockwool, mineral wool or any other suitable insulating medium. It may alsobe preferred in some applications to house the primary plant materialseparator 8 within a vacuum jacket. By way of example only, such avacuum jacket would look substantially similar to the heating jacket 36illustrated in FIG. 9, except there would be no entry 37 or exitpassages 38 for a heating medium. Instead, an evacuation passage wouldbe included that may include a check valve or similar vacuum containmentmethod. Alternatively, the vacuum jacket may be permanently sealed orwelded closed to retain the vacuum. The primary plant material separatorand/or separated plant material exit tube 44 may also be housed withinan insulated and/or heated chamber with all or some of the heatedcomponents of the system. Such a method has been described in detail inother sections of this disclosure.

In some cases, more efficient collection of the volatilized plant oilsmay occur through the utilization of a wetted packing material 81.Non-limiting examples of embodiments that utilize wetted packingmaterials are discussed in PCT/IB2014/002383, which is incorporatedherein in its entirety, by reference. One example of a collectionchamber containing wetted packing is illustrated in FIG. 10. Such anembodiment utilizing wetted packing may include a collection chamber 80containing a wetted substrate 81 such as, but not limited to, randompacking including Raschig rings, saddles and beads made of glass,ceramics metals or other materials, other random packing materials suchas sand, alumina, gravel, PTFE fibers, stainless steel wool, fiberglassor mineral wool fibers, and structured packing such as knitted packing,woven wire mesh, stainless steel wool, stainless steel matting, wovenstainless steel mesh, corrugated metal sections, bubble-cap plates andsieve tray plates or other types of packing to capture the volatilizedplant oils. The packing material 81 may be wetted with collectionsolvent, which may collect the plant oils and eventually drip downthrough the packing material to the sump area 13 to be recovered. InFIG. 10, the packing material may be wetted by collection solventsprayers 82 or by other methods of contacting the packing material withcollection solvent. As with other embodiments, it should be known thatthe wetted packing collection chamber 80 illustrated in FIG. 10 may alsoserve as the system's cooling chamber, with the sprayers 82 and/orpacking material 81 serving to cool the gas stream. Alternatively, aseparate cooling chamber may be provided upstream of the collectionchamber 80, as is already illustrated in FIG. 10. A collection chamberwith a wetted packing material may be used in other embodiments and incombination with collection chambers with collection solvent sprayers 17or any other collection methods. The location of the collection chamber80 may also be varied depending on the application. As one non-limitingexample, the wetted packing collection chamber 80 may be relocated tothe position of the gas stream cooler 50.

Finally, it should be known that in addition to the oil dropletcollection methods previously discussed, an electrostatic method ofcapturing condensed oil droplets may also be employed in the presentinvention. In such embodiments, an electrostatic scrubber, the design ofwhich will be readily known to those who are skilled in the art, may beplaced after the cooling section 9 of the system. With this placement,the electrostatic collection plates may be optionally washed ofcollected oils by the falling collection solvent. The electrostaticcollection plates may also be placed after the agglomeration section 14or after the collection chamber section 16 and may be optionally washedwith a spray of collection solvent. If efficient electrostaticcollection occurs, it may be possible to reduce or eliminate some of theother collection methods throughout the system.

By way of non-limiting example only, the following operating conditionsand delivery rates may be utilized to extract plant oil: Acentrifugal-type gas stream mover 19 capable of providing an outletpressure of approximately 1.0 to 5.0 pounds per square inch is utilizedto move the gas stream 1 throughout the system. Other examples mayinclude a gas stream mover capable of providing an outlet pressure of 0to 150 pounds per square inch. The gas stream mover 19 moves the gasstream 1 throughout the system at a flow rate of approximately 30 to 100standard cubic feet per minute. Other examples may include a gas streammover capable of providing a flow rate of approximately 0.1 to 30standard cubic feet per minute, 100 to 200 standard cubic feet perminute, 200 to 500 standard cubic feet per minute, over 500 cubic feetper minute or other ranges. As the gas stream passes through the gasstream heater 2, the gas stream is heated to a temperature ofapproximately 290 to 430 degrees Fahrenheit. In other examples, the gasstream may be heated to a temperature range of approximately 100 to 300degrees Fahrenheit, 100 to 310 degrees Fahrenheit, 200 to 300 degreesFahrenheit, 200 to 310 degrees Fahrenheit, 280 to 450 degreesFahrenheit, 300 to 500 degrees Fahrenheit, 300 to 400 degreesFahrenheit, 300 to 370 degrees Fahrenheit, 300 to 365 degreesFahrenheit, 305 to 360 degrees Fahrenheit, 300 to 360 degreesFahrenheit, 300 to 330 degrees Fahrenheit, 310 to 320 degreesFahrenheit, 340 to 370 degrees Fahrenheit, 350 to 360 degreesFahrenheit, 350 to 365 degrees Fahrenheit, 415 to 445 degreesFahrenheit, any combination of these temperature ranges or othertemperature ranges. Powdered or finely-ground plant material containingplant oils is fed into the gas stream 1 via an entrainment zone 6 at arate of approximately 0.03 to 0.25 pounds per minute. Other examples mayinclude a feed rate of 0.001 to 0.03 pounds per minute, 0.25 to 1.0pounds per minute, 1.0 to 5.0 pounds per minute, 5.0 to 10.0 pounds perminute, more than 10.0 pounds per minute or other feed rates. To thegreatest degree possible, the internal surface temperature of theextraction chamber 7 area and all areas of the system that contact thegas stream as the gas stream passes between the gas stream heater 2 andthe gas stream cooling section 9 are kept above the condensationtemperature of the volatilized oils or near the temperature of the gasstream exiting the heater 2 to prevent condensation of plant oils onthese surfaces. In some examples, this temperature is kept near or aboveapproximately 290 to 430 degrees Fahrenheit. In other examples, thetemperature may be kept in a range of approximately 100 to 300 degreesFahrenheit, 100 to 310 degrees Fahrenheit, 200 to 300 degreesFahrenheit, 200 to 310 degrees Fahrenheit, 280 to 450 degreesFahrenheit, 300 to 500 degrees Fahrenheit, 300 to 400 degreesFahrenheit, 300 to 370 degrees Fahrenheit, 300 to 365 degreesFahrenheit, 305 to 360 degrees Fahrenheit, 300 to 360 degreesFahrenheit, 300 to 330 degrees Fahrenheit, 310 to 320 degreesFahrenheit, 340 to 370 degrees Fahrenheit, 350 to 360 degreesFahrenheit, 350 to 365 degrees Fahrenheit, 415 to 445 degreesFahrenheit, any combination of these temperature ranges or othertemperature ranges. The evaporation device 31 is operable to distillapproximately 0.04 to 0.15 gallons per minute of collection solvent fromthe mixture of plant oils and collection solvent. Other examples mayinclude separation rates of approximately 0.0002 to 0.04 gallons perminute, 0.15 to 0.5 gallons per minute, 0.5 to 1.0 gallons per minute,1.0 to 5.0 gallons per minute, 5.0 to 10.0 gallons per minute, more than10.0 gallons per minute or other rates. The distilled collection solventis stored in a separate reservoir 56 from the sump reservoir area 13. Asubstantially purified flow of collection solvent is pumped to thecooling spray 10 at a rate of approximately 0.03 to 1.0 gallons perminute. Other examples may include rates of 0.0002 to 0.03 gallons perminute, 1.0 to 7.0 gallons per minute, 7.0 to 10.0 gallons per minute,greater than 10.0 gallons per minute, less than 10.0 gallons per minuteor other rates. The cooling spray cools the gas stream to approximately160 to 180 degrees Fahrenheit. In other examples, the cooling spraycools the gas stream to approximately 80 to 150 degrees Fahrenheit, 0 to150 degrees Fahrenheit, 0 to 100 degrees Fahrenheit, 40 to 80 degreesFahrenheit, less than 180 degrees Fahrenheit, less than 173 degreesFahrenheit, less than 150 degrees Fahrenheit, less than 140 degreesFahrenheit, less than 130 degrees Fahrenheit, less than 120 degreesFahrenheit, less than 110 degrees Fahrenheit, less than 100 degreesFahrenheit or other temperatures. After contacting the cooling spray,the gas stream and entrained liquids pass through the primary gas streamcooler 50. The gas stream cooler 50 cools the gas stream and entrainedliquids/oils to approximately 90 to 150 degrees Fahrenheit. In otherexamples, the gas stream cooler cools the gas stream and entrainedliquids/oils to approximately 0 to 150 degrees Fahrenheit, 0 to 100degrees Fahrenheit, 40 to 80 degrees, 0 to 90 degrees Fahrenheit, lessthan 150 degrees Fahrenheit, less than 140 degrees Fahrenheit, less than130 degrees Fahrenheit, less than 120 degrees Fahrenheit, less than 110degrees Fahrenheit, less than 100 degrees Fahrenheit, less than 90degrees Fahrenheit, less than 80 degrees Fahrenheit, or othertemperatures. In embodiments using only a spray cooler or a spraycollection chamber to cool the gas stream, these sections may beoperable to cool the gas stream and entrained liquids/oils toapproximately 90 to 150 degrees Fahrenheit or any of the temperatureranges listed above for the cooling spray or gas stream cooler. Inembodiments in which the collection solvent is cooled by a cooler, suchas 55, before being sprayed in the spray cooler, the collection solventmay be cooled to a temperature less than the boiling point of thecollection solvent being used. In other examples, the collection solventcooler, such as 55, may cool the collection solvent to a temperature ofapproximately 0 to 150 degrees Fahrenheit, 0 to 40 degrees Fahrenheit,40 to 80 degrees Fahrenheit, 80 to 120 degrees Fahrenheit, to less than100 Fahrenheit, to less than 120 degrees Fahrenheit, to less than 150degrees Fahrenheit or other temperature ranges. To the greatest degreepossible, all of the internal areas of the system that contact the gasstream as the gas stream passes between the gas stream cooler 50 and thegas stream heater 2 are kept at a temperature that is below thetemperature of the gas stream when it exits the gas stream cooler 50,such that collection solvent condenses on these surfaces to wash awayany accumulated plant oils. In some examples, the temperature is keptnear or below 85 to 145 degrees Fahrenheit. The primary solvent pump 12pumps collection solvent from the sump area 13 to the collection solventsprayers 17 in the collection chamber 16 at a rate of approximately 1.0to 7.0 gallons per minute. Other examples include a rate of 0.0002 to1.0 gallons per minute, 7.0 to 10.0 gallons per minute, greater than10.0 gallons per minute, less than 10.0 gallons per minute or otherrates. The collection solvent used within the system may be comprisedprimarily of ethyl alcohol and water at a ratio of approximately 40%ethyl alcohol and 60% water to 95% ethyl alcohol and 5% water. Theevacuation pump 24 is operable to maintain a negative system pressuresuch that the highest pressure area of the gas stream (such as thatfound at the blower exit) is still kept slightly below that of ambientpressure. In doing such, solvent vapors and/or volatilized plant oils donot readily escape from the seals within the system and must passthrough the cold trap 22 where they are condensed and returned to thesystem. The volume of gas displaced by the evacuation pump 24 isapproximately 0.01 to 5.0 cubic feet per minute.

The specific descriptions in this disclosure should not be viewed aslimiting the scope of this invention. As a non-limiting example,different heat exchangers may be used, components may be moved around,functions of various components may be combined into one structure orthe function of one component may be divided between several components.Further, the arrangements and configurations of elements in FIG. 1 andFIG. 2 are for ease of explanation and are not limiting. As one example,the volatilization chamber 7 is shown with a bottom entrance and a topexit but may have the entrance and exit located elsewhere. Those ofskill in the art will recognize that the herein described embodiments ofthe present invention may be altered in other ways without departingfrom the scope or teaching of the present invention. As anothernon-limiting example of one of many ways that the system may berearranged, in comparison to FIG. 1, the embodiment illustrated in FIG.2 shows several of the parts of the system rearranged or eveneliminated. FIG. 2 shows that the centrifugal droplet separator 20illustrated in FIG. 1 has been removed. In this embodiment, only asingle demisting section 21 is utilized to prevent droplets fromentering the heater 2. The steam generator 3 has also been removed inFIG. 2. In this embodiment, electric heating elements are used in theheater section 2. The plant material collection system has also beensimplified. Instead of utilizing a secondary entrainment zone 27 and asecondary gas stream 25, the primary plant material separation devicedrains directly into the processed plant material collection bin 29. Anoptional airlock valve 58 may be used to keep the processed plantmaterial collection bin 29 separated from the primary gas stream 1. Twogas movers 19 have been used in series to increase the pressureavailable to propel the gas stream. The placement of one of the gasmovers 19 has been moved from the position illustrated in FIG. 1,however, this could be placed directly in front of the second gas mover19 or elsewhere in the system.

FIG. 11 illustrates an embodiment of the invention that is designed tooperate without a collection solvent. This embodiment may be operatedwith no solvent at all, or with only a minimal amount of a dilutingsolvent. This embodiment includes a primary gas stream 1, atube-in-shell steam powered gas stream heater 2, a steam generator 3 toprovide steam to the heater, a gas stream mover 19, a hopper 4, a plantmaterial portioning device 5, a primary plant material entrainment zone6, one or more volatilization chambers 7, a primary plant materialseparation device 8, a gas stream filter 49, a volatilized oilcondenser/gas stream cooler 50, a condensed plant oil gas stream/oilseparation device 82, an oil collection area 32, a heated separatedplant material exit 44, an air pump 24 capable of removing a portionedamount of gas from the system, a secondary gas stream 25, a secondarygas stream mover 26, a secondary plant material entrainment zone 27, asecondary plant material separation device 28, a processed plantmaterial collection bin 29, and an in-only check valve 30 to allowatmospheric air or a displacing gas into the system via the plantmaterial collection bin 29. Depending on the desired application, any ofthese components and parts may be duplicated within the system one ormore times in series or in parallel or may be eliminated entirely toattain different effects. The order of the components within the systemmay also be modified to attain different effects. The steam poweredheater 2 may also be replaced with an electrically powered heater, aheater with a circulating thermal fluid, or a heater that is powered byother methods. Elements 1, 2, 3, 19, 4, 5, 6, 7, 8, 49, 44, 25, 26, 27,28, 29, 30, 22, 23, and 24 function in a substantially similar manner tocorresponding similar components in previously discussed embodiments ofthe invention. Element 50, however, functions in a modified way ascompared to previously discussed embodiments. Additionally, in someembodiments, the gas stream mover has been placed after the heater suchthat it remains too hot for plant oils to condense on its innersurfaces. It should be noted that the elements mentioned may alsofunction in a similar way in the embodiments following this section.

The embodiment illustrated in FIG. 11 is designed to use little or nosolvent. After the volatilized plant oils travel from the volatilizationsection 7, through the primary plant material separation device 8 andthrough the optional gas stream filter 49, they enter a volatilized oilcondenser/gas stream cooling section 50. The condenser/gas stream cooler50 is preferably a tube-in-shell heat exchanger that is cooled by acoolant or coolant mixture, however, any of the condenser designs andcooling methods previously discussed within this document orPCT/IB2014/002383 may be used. As the volatilized oils enter the gasstream condenser/cooler 50, a portion of the volatilized oils condenseon the condensation surfaces within the condenser. The volatilized oilsthat do not condense through the first pass through the condenser maycontinue to recirculate with the gas stream until they are condensed insuccessive passes through the condenser 50. The extracted plant oilsthat condense on the condensation surfaces within the condenser 50 dripdown the condenser surfaces and flow out of the condenser 50 into acondensed oil separation section 82 and eventually into the condensedoil collection area 32. The gas stream 1 continues to flow through thesystem and back through the heater.

It is beneficial to maintain the coolant medium and/or condensationsurfaces within the gas stream condenser/gas stream cooler 50 at atemperature that is below the condensation point of the volatilizedplant oils being extracted and yet still high enough to keep the plantoils in a runny state so they readily drip and flow out of the bottom ofthe condenser 50, through the condensed oil separation section 82 andinto the condensed oil collection area 32. A few non-limitingtemperature examples may include maintaining the condensation surfaceswithin the condenser between 100 to 300 degrees Fahrenheit, 120 to 280degrees Fahrenheit, 120 to 150 degrees Fahrenheit, and 320 to 340degrees Fahrenheit. Other temperatures ranges may also be used.

FIG. 12a illustrates another embodiment of the invention that needslittle or no solvent to function. In this embodiment, a centrifugalcondensed oil separator 83 is utilized. The centrifugal oil separator 83may be a cyclone or other suitable separation device. As the gas streampasses through the gas stream condenser/cooler 50, a portion of thevolatilized plant oils will condense on the surfaces within thecondenser, however, a portion of the oil may also condense andprecipitate into the cooler gas stream as small or microscopic oildroplets that become entrained in the flow of the gas stream. By using acentrifugal oil separator 83, a large portion of these entrained smalland microscopic oil droplets are captured within the oil separator priorto being recirculated back through the heater 2. The oil droplets thatare captured, along with the oil that drips from the condenser 50, maythen drain into the extracted oil collection area 32. In order toillustrate that many of the components within the invention may berearranged or altered in different applications, the embodimentillustrated in FIG. 12a is shown with a simplified processed plantmaterial collection system as compared to FIG. 11.

FIG. 12b illustrates an arrangement similar to the embodimentillustrated in FIG. 12a . In this embodiment, the gas stream mover 19 isplaced after the condenser/cooler 50 and before the heater 2. Anoptional condensed oil separation section 82 may be included in thisembodiment. It is preferred that the gas stream mover be of acentrifugal blower design, such as, but not limited to a regenerativeblower, turbine blower, pressure blower, turbo compressor, centrifugalblower or any other design capable of creating suitable centrifugalforces. By positioning a centrifugal type gas stream mover 19 after thegas stream cooler 50, the gas stream mover 19 serves as a centrifugaloil separator that separates and collects microscopic oil droplets thatprecipitated into the gas stream after the gas stream was cooled. Theoil droplets that are captured in the gas stream mover 19, along withany oil that drips from the condenser 50, may then drain into theextracted oil collection area 32. A gas stream mover with blades (e.g.,a turbo compressor, regenerative blower, turbine blower, pressure bloweror a gas stream mover with high speed parts) may also collect oildroplets by impingement when the oil droplets collide with surfaces ofthe blades. Such a blower may be substituted for any of the gas streammover elements discussed in this document.

In the embodiments illustrated in FIGS. 12a and 12b , it is preferablethat the centrifugal oil separator 83 or centrifugal gas stream mover 19be maintained at a temperature that is high enough to keep the captureddroplets runny and free flowing so the collected oil may flow from thecentrifugal capture device, yet cool enough to prevent any of thecaptured oil droplets from being re-volatilized. It is also preferablethat the condenser/gas stream cooler 50 in the embodiments illustratedin FIGS. 12a and 12b be maintained at a temperature below thecondensation point of the volatilized plant oils being extracted and yetstill high enough to keep any collected oil in a runny state so theyreadily drip and flow out of the bottom of the condenser 50 and continueto flow through the system and into the extracted oil collection area32. In some embodiments illustrated in FIGS. 12a and 12b , it may bepreferred to design the gas stream cooler 50 to minimize the quantity ofoil collected in the condenser and rely primarily on the centrifugalseparator 83 or centrifugal gas mover 19 as the primary separationdevice.

FIG. 13 illustrates another embodiment that is designed to use little orno solvent to function. In this embodiment, a set of elements thatincludes a gas stream condenser/cooler 50, an oil separator 82 and anextracted oil collection area 32 is repeated in series as many times asis practical to remove various fractions from the volatilized oilswithin the gas stream. With this arrangement, fractionalization of theplant oil constituents may occur in a continuous manner. For ease ofexplanation, only two sets of gas stream condensers/coolers 50, oilseparation sections 82 and extracted oil collection areas 32 areillustrated in FIG. 13, however, this number may be increased. In theembodiment illustrated in FIG. 13, it will be beneficial to set theheater 2 to a temperature that is high enough to volatilize all of thedesired fractions within the plant material to be extracted, such thatall of the oil fractions become volatilized and travel within the gasstream 1 as volatilized plant oil gasses. The condensation surfaceswithin the first gas stream condenser/cooler 50 should be maintained ata temperature that is low enough to condense a first fraction ofvolatilized plant oil constituents and yet is too high to condense otherfractions of volatilized plant oil constituents. The first fraction ofvolatilized plant oils will condense on the condenser surfaces and drainthrough the first condenser 50, through the first oil separator 82 andinto first oil collection area 32. Other fractions within thevolatilized oil entrained in the gas stream that have lower condensationpoints than the first fraction of volatilized plant oils cannot condensewithin the first condenser 50 and will continue to travel within the gasstream as a volatilized plant oil gas into a second gas streamcondenser/cooler 50. The condensation surfaces within the second gasstream condenser/cooler 50 are maintained at a temperature that is lowerthan the first gas stream condenser/cooler 50 and also low enough tocondense a second fraction of volatilized plant oil constituents and yetalso too high to condense other volatilized plant oil constituents. Thispattern may be repeated with multiple gas stream condenser/coolers asmany times as is practical to remove various fractions from thevolatilized oils within the gas stream. It is beneficial that the lastcondenser 50 in the series be maintained at a low enough temperature tocondense all of the remaining oil fractions and yet still be kept hotenough to keep the oils flowing freely from the last condenser, throughthe last oil separator 82 and into the last extracted oil collectionarea 32.

FIG. 14 illustrates an additional embodiment that enables continuousfractionalization. In this embodiment, the last oil separation device inthe series is a centrifugal oil separation device 83, as previouslydescribed in the section describing FIG. 12a . A centrifugal separationdevice 83 may be placed after each successive condenser/gas streamcooler 50 to facilitate collection of the fractionated oil components ina similar way as described in FIG. 12 a.

FIG. 15 illustrates an additional embodiment that enables continuousfractionalization. In this embodiment, the gas stream mover 19 has beenrelocated to serve as a centrifugal oil separation device. In thisembodiment, it is beneficial to utilize a centrifugal type gas streammover that generates high centrifugal effects. Examples of centrifugalgas movers have been previously discussed in other sections of thisdisclosure. A few non-limiting examples may include turbo compressors,regenerative blowers, turbo blowers, pressure blowers and othercentrifugal devices. A centrifugal gas stream mover 19 may be placedafter each successive condenser 50 to facilitate collection of thefractionated oil components.

As non-limiting examples of potential temperatures that may be utilizedin the embodiments illustrated in FIGS. 13, 14, and 15, the followingapproximate temperatures may be beneficial: The internal areas of thevolatilization chamber may be heated to a temperature between 356 and440 degrees Fahrenheit to volatilize all of the desired fractions ofplant oil to be extracted. The condensation surfaces within a first gasstream condenser/cooler 50 may be maintained between 366 and 427 degreesFahrenheit. The condensation surfaces within a second gas streamcondenser/cooler may be maintained between 357 and 364 degreesFahrenheit. The condensation surfaces within a third gas streamcondenser/cooler 50 may be maintained between 316 and 355 degreesFahrenheit. The condensation surfaces within a fourth gas streamcondenser/cooler 50 may be maintained between 290 and 314 degreesFahrenheit. The condensation surfaces within a final gas streamcondenser/cooler 50 may be maintained between 110 and 289 degreesFahrenheit. Other temperatures and numbers of repeating components maybe used in other embodiments and examples.

As alternative non-limiting examples of potential temperatures that maybe utilized in the embodiment illustrated in FIGS. 13, 14 and 15 thefollowing approximate temperatures may be beneficial: The internal areasof the volatilization chamber may be heated to a temperature between 356and 400 degrees Fahrenheit to volatilize all of the desired fractions ofplant oil to be extracted. The condensation surfaces within a first gasstream condenser/cooler 50 may be maintained between 357 and 364 degreesFahrenheit. The condensation surfaces within a second gas streamcondenser/cooler may be maintained between 316 and 355 degreesFahrenheit. The condensation surfaces within a third gas streamcondenser/cooler 50 may be maintained between 290 and 314 degreesFahrenheit. The condensation surfaces within a final gas streamcondenser/cooler 50 may be maintained between 110 and 289 degreesFahrenheit. Other temperatures and numbers of repeating components maybe used in other embodiments and examples.

FIG. 16 illustrates an embodiment that utilizes an electrostaticcollector 84 to efficiently remove plant oil from the gas stream. As thegas stream passes through the gas stream condenser/cooler 50, a portionof the volatilized plant oils may condense on the surfaces within thecondenser and drip down through the system and into the extracted oilcollection area 32, while another portion of the oil may condense andprecipitate into the cooler gas stream as small or microscopic oildroplets that become entrained in the flow of the gas stream. By usingan electrostatic collector 84, a large portion of these entrained smalland microscopic oil droplets may be captured within the electrostaticcollector prior to being recirculated back through the heater 2. As thegas stream and entrained small and microscopic plant oil droplets passfrom the gas stream condenser 50 and enter the electrostatic collector84, the electrostatic collector 84 imparts an electrostatic charge tothe entrained oil droplets. The collection surfaces within theelectrostatic collector 84 are charged with an opposite electrostaticcharge from the oil droplets. As the entrained oil droplets pass nearthe collection surfaces, the oil droplets are electrically attracted tothe collection surfaces. As the oil droplets collect on the collectionsurfaces, they begin to coalesce into larger droplets that drip from theelectrostatic collection surfaces and drain through the system into theextracted oil collection area 32. The design and function ofelectrostatic collectors will be known to those of skill in the art.

In the embodiment illustrated in FIG. 16, it is beneficial that thecondensation surfaces within the gas stream condenser/cooler 50 bemaintained at a temperature below the condensation point of thevolatilized plant oils being extracted and yet high enough to keep theplant oils in a runny state so they readily drip and flow out of thebottom of the condenser 50, through the electrostatic collector 84,through the condensed oil separation section 82 and into the condensedoil collection area 32. In order for collected plant oils to easily flowfrom the electrostatic collector 84, it is beneficial that the gasstream exiting the gas stream condenser/cooler 50 be maintained at atemperature that keeps the surfaces of the electrostatic collector 84warm enough that collected oil may freely drip from the electrostaticcollection surfaces and drain down through the system to the oilcollection area 32. A few non-limiting temperature examples may includemaintaining the condensation surfaces within the condenser 50 andelectrostatic collector area 84 between 100 to 300 degrees Fahrenheit,120 to 280 degrees Fahrenheit, 120 to 150 degrees Fahrenheit, and 320 to340 degrees Fahrenheit. In some embodiments illustrated in FIG. 16, itmay be preferred to design the condenser/gas stream cooler 50 tominimize the quantity of oil collected in the gas stream cooler 50 andrely primarily on the electrostatic collector 84 as the primary oilcollection/separation device.

FIG. 17 illustrates an embodiment that utilizes a filtration section 85that includes filters, demisting pads and/or packing material to removesmall and microscopic oil droplets from the gas stream. The mediumscontained in the filtration section 85 are designed to function withlittle or no solvent. Since there may be little or no solvent present,it is preferred that the filtration section be maintained at atemperature that keeps the collected oil runny and free flowing so as toallow the oil to easily drip from the filter and/or demisting pads andinto the extracted oil collection area 32. As the gas stream passesthrough the gas stream condenser/cooler 50, a portion of the volatilizedplant oil may condense on surfaces within the condenser and drip downthrough the system and into the extracted oil collection area 32, whileanother portion of the oil may condense and precipitate into the coolergas stream as small or microscopic oil droplets that become entrained inthe flow of the gas stream. As the gas stream and entrained small andmicroscopic plant oil droplets pass from the gas stream condenser 50 andpass through the filtration section 85, a portion of the entrained oildroplets may be removed from the gas stream. The filtration material maycomprise a number of materials, such as, but not limited to sinteredglass filters, sintered ceramic filters, sintered metal filters, ceramicfilters, other filter designs, random and/or inert packing includingRaschig rings, saddles and beads made of glass, ceramics, metals, otherrandom and/or inert packing materials such as sand, alumina, gravel,PTFE fibers, stainless steel wool, glass fibers or mineral wool fibers,and structured packing such as knitted packing, woven wire mesh,stainless steel wool, stainless steel matting, woven stainless steelmesh, corrugated metal sections, bubble-cap plates and sieve tray platesor other types of packing to capture the volatilized plant oils. Thedemisting material may comprise any of the preceding materials, or thedemisting material may comprise a structured demister design, corrugatedplates demister design, or other design.

Portions of the systems in FIGS. 11, 12 a, 12 b, 13, 14, 15, 16 and 17may be heated and/or insulated to assist in achieving targettemperatures and/or to prevent condensation in certain areas of thesystem.

Any of the embodiments illustrated in FIGS. 11, 12 a, 12 b, 13, 14, 15,16 and 17 and discussed in their accompanying text may use little or nosolvent to function. In some cases, it may be preferred to useno-solvent. In some cases, it may be preferred to use a minimal amountof solvent, not as a primary collection method, but as a diluent orthinning agent to maintain a liquefied oil in a free-flowing state suchthat it freely drains from the invention's various collection andseparation devices. In cases where a minimal amount of solvent isutilized, the general goal is to use as little as possible. A fewnon-limiting examples would be to use a sufficient amount of solventsuch that the collected oils can be measured to contain 25% or lesssolvent by weight, 15% or less solvent by weight or 10% or less solventby weight. It may also be advantageous in some cases to maintain acertain level of dissolved solvent in the gas stream. A few non-limitingexamples would be to use a sufficient amount of solvent such that thegas stream can be measured to contain 25% or less solvent vapor byweight, 15% or less solvent vapor by weight or 10% or less solvent vaporby weight. In other cases, it may be preferred to maintain a much higherratio of diluting solvent to ensure that the collected oils do notbecome too thick to be removed from the system.

The introduction of diluting solvent to the embodiments illustrated inFIGS. 11, 12 a, 12 b, 13, 14, 15, 16 and 17 may be before and/or withinthe gas stream cooler 50, before and/or within the centrifugalcollection device section 83, before and/or within the centrifugal gasstream mover collection section 19, before and/or within theelectrostatic collection section 84, before and/or within the filtercollection section 85, before and/or within the oil separation section82, and/or within other sections of the system. In some embodiments, itmay be advantageous to introduce the diluting solvent as a vapor insteadof a liquid, with the point of introduction being placed in any of thesections previously stated, within the gas stream 1, within the gasstream heater 2, within the extraction chamber 7, within the gas streammover 19, within the gas stream filter 49, within the plant materialseparation device 8, and/or anywhere within the system. The method ofintroduction of a diluting solvent may be via a nozzle, tube, sprayer,valve, gas injector or any other method known to those of skill in theart or described in other parts of this disclosure.

The diluting solvent utilized in the embodiments illustrated in FIGS.11, 12 a, 12 b, 13, 14, 15, 16 and 17 may consist of ethanol, a mixtureof ethanol and water, or may consist of any of compounds that are usedas collection solvents in any other embodiments described within thisdisclosure or PCT/IB2014/002383, or other solvents, or a mixture ofvarious solvents. It is preferred that the diluting solvent be food ormedical grade, however any suitable diluting solvent may be used. Ifethanol is introduced as the diluting solvent, a few non-limitingexamples may to introduce an ethanol diluting solvent that is about 100%ethanol, about 95% ethanol and 5% water, about 90% ethanol and 10%water, about 85% ethanol and 15% water, about 80% ethanol and 20% water,about 75% ethanol and 25% water, about 70% ethanol and 30% water, about65% ethanol and 35% water, about 60% ethanol and 40% water, about 55%ethanol and 45% water, about 50% ethanol and 50% water, or ethanol andwater at other ratios. Alternatively, if ethanol is introduced as thediluting solvent, a mixture of ethanol and water may be introduced withan ethanol concentration that is greater than 40% ethanol, greater than50% ethanol, greater than 55% ethanol, greater than 65% ethanol, greaterthan 70% ethanol, greater than 75% ethanol, greater than 80% ethanol,greater than 85% ethanol, greater than 90% ethanol or greater than 95%ethanol. Ethanol may also be mixed with other solvents at variousratios. The specific descriptions in this disclosure should not beviewed as limiting the scope of this invention. The elements within theembodiments illustrated in FIGS. 11, 12 a, 12 b, 13, 14, 15, 16 and 17,along with other elements discussed in the text describing the same, orelements discussed in text or illustrated in figures from any othersection of this disclosure, may be rearranged in different orders withinthe system, combined with different elements described in otherembodiments, repeated in parallel or in series, or may be eliminatedentirely in some embodiments. As a non-limiting example, different heatexchangers and heaters may be used, components may be moved around,functions of various components may be combined into one structure orthe function of one component may be divided between several components.Further, the arrangements and configurations of elements in FIGS. 11, 12a, 12 b, 13, 14, 15, 16 and 17 are for ease of explanation and are notlimiting. As one example, the volatilization chamber 7 is shown with abottom entrance and a top exit but may have the entrance and exitlocated elsewhere. It should be noted that the gas streamcondenser/cooler 50 and electrostatic collector 84 may be combined intothe same section in some embodiments. It should also be noted that thegas stream heater 2 may be powered by electric heating elements insteadof steam or a heated fluid. Other condenser designs may be used. Any ofthe components described in FIGS. 11, 12 a, 12 b, 13, 14, 15, 16 and 17and their accompanying text may be modified in any way that similarcomponents are described in other embodiments within this disclosure,PCT/IB2014/002383, or in other ways that are generally known to those ofskill in the art. Additionally, in some cases, it may be advantageous tooperate the embodiments in FIGS. 11, 12 a, 12 b, 13, 14, 15, 16 and 17as open systems. In cases where the embodiments illustrated in FIGS. 11,12 a, 12 b, 13, 14, 15, 16 and 17 are operated as open systems, it ispreferable that the system be open after the final oil dropletseparator/collection device (83, 19, 84, 85 or 82) and before the heater2.

In some aspects, the disclosure relates to a method of extracting oilfrom plant material. The method may comprise providing a system forextracting oil from plant material. The system may comprise a gas movingdevice operable to propel a gas stream through the system. The systemmay comprise an extraction chamber in communication with the gas movingdevice such that the gas stream is directed through the extractionchamber. The system may comprise a condensation surface in communicationwith the gas moving device such that the gas stream is directed to thecondensation surface.

The gas moving device may or may not be a centrifugal separator. The gasmover may or may not comprise a compressed air tank or a liquefied gas,such as liquid nitrogen.

The condensation surface may be a surface configured to allow theportion of oil to flow along the surface to allow collection of the oil.The condensation surface may therefore comprise chemical and/ormechanical properties that allow the portion of oil to flow. Acondensation surface that allows the portion of oil to flow provides anadvantage over existing systems because it allows methods that use lesssolvent.

The system may comprise a centrifugal separator, which may comprise thecondensation surface. The centrifugal separator may or may not be thegas moving device of the system. The centrifugal separator may compriseat least one blade and an axis of rotation, e.g., such that the at leastone blade rotates about the axis, or the centrifugal separator maycomprise a device with no blades at all. The method may further compriserotating the blade about the axis. The condensation surface may comprisethe at least one blade and/or may comprise a surface of the centrifugalseparator other than a blade such as the housing of the separator.Contacting the gas stream with the condensation surface may cause theportion of oil to collect on a blade, housing, and/or other surface ofthe centrifugal separator. The method may further comprise maintainingthe at least one blade at both a temperature and an angular velocitythat results in a centrifugal force that is greater than the resistanceof the portion of the oil to flow. The rotation of the blade about theaxis may thereby provide a mechanical force that causes the portion ofthe oil to flow such that the oil may be collected.

In some embodiments, the condensation surface does not comprise a bladeof the centrifugal separator. For example, a system may comprise acentrifugal separator that lacks blades, or a system may comprise acentrifugal separator having one or more blades wherein the condensationsurface does not comprise the one or more blades.

The system may comprise a condensation surface that is heated and/orangled to allow the portion of oil to flow. A method may comprisemaintaining a condensation surface at an angle and temperature thatresult in a parallel component of gravitational force that is greaterthan the resistance of the portion of the oil to flow. The condensationsurface may be angled of about −90° to about 90° relative to the forceof gravity, such as about −90° to about −70°, about −80° to about −60°,about −70° to about −50°, about −60° to about −40°, about −50° to about−30°, about −40° to about −20°, about −30° to about −10°, about −20° toabout 0°, about −10° to about 10°, about 0° to about 20°, about 10° toabout 30°, about 20° to about 40°, about 30° to about 50°, about 40° toabout 60°, about 50° to about 70°, about 60° to about 80°, or about 70°to about 90°. Surfaces of less than 0° to about −90° are ceilings, asurface of 0° is a wall that is parallel to the force of gravity, andsurfaces of greater than 0° to less than 90° are inclined planes. Thecondensation surface may be angled at about −90° to about 60°, about 0°to about 60°, about 0° to about 45°, or about −45° to about 45° relativeto the force of gravity.

A condensation surface may comprise an electrostatic charge. Theelectrostatic charge may be sufficient to capture and remove a portionof the oil from the gas stream. The method may further comprisecondensing the portion of the oil into oil droplets that becomeentrained in the gas stream after volatizing the oil. In someembodiments, the method comprises charging the oil droplets with anelectrostatic charge (e.g., a charge that is opposite from the charge ofthe condensation surface). Contacting the gas stream with thecondensation surface may comprise contacting the charged oil dropletswith the condensation surface.

A condensation surface may comprise a filter medium and/or demistingpad. The filter medium and/or demisting pad may be sufficient to captureand remove a portion of the oil from the gas stream. The method mayfurther comprise condensing the portion of the oil into oil dropletsthat become entrained in the gas stream after volatizing the oil.

In some embodiments, the temperature of a condensation surface,centrifugal separator, centrifugal capture device, centrifugal gasstream mover, electrostatic collector, filter section, condenser, and/orgas stream cooler is about 100° F. to about 300° F., about 110° F. toabout 289° F., about 120° F. to about 280° F., about 120° F. to about150° F., about 290° F. to about 314° F., about 316° F. to about 355° F.,about 320° F. to about 340° F., about 357° F. to about 364° F., or about366° F. to about 427° F. The temperature of a condensation surface,centrifugal separator, centrifugal capture device, centrifugal gasstream mover, electrostatic collector, filter section, condenser, and/orgas stream cooler may be about 100° F. to about 315° F., about 100° F.to about 212° F., or about 120° F. to about 315° F. The temperature of acondensation surface, centrifugal separator, centrifugal capture device,centrifugal gas stream mover, electrostatic collector, filter section,condenser, and/or gas stream cooler may be about 100° F. to about 140°F., about 120° F. to about 160° F., about 140° F. to about 180° F.,about 160° F. to about 200° F., about 180° F. to about 220° F., about200° F. to about 240° F., about 220° F. to about 260° F., about 240° F.to about 280° F., about 260° F. to about 300° F., about 280° F. to about320° F., about 300° F. to about 340° F., about 320° F. to about 360° F.,about 340° F. to about 380° F., about 360° F. to about 400° F., about380° F. to about 420° F., or about 400° F. to about 440° F.

A system may comprise more than one condensation or collection surface,and one condensation or collection surface may be kept at a differenttemperature than another condensation or collection surface. In suchembodiments, any of the temperature ranges infra may be usedinterchangeably with different components. As a non-limiting example, itmay be preferred to keep the temperature of the condenser/gas streamcooler section 50 within a higher temperature range than the centrifugalcollection device section 83, centrifugal gas stream mover collectionsection 19, electrostatic collection section 84 or filter collectionsection 85, and, in some cases, it may be preferred to keep thetemperature of the condenser/gas stream cooler section 50 within a lowertemperature range than the centrifugal collection device section 83,centrifugal gas stream mover collection section 19, electrostaticcollection section 84 or filter collection section 85.

In general, it is desirable to maintain the collection surfaces of theembodiments illustrated in FIGS. 11, 12 a, 12 b, 13, 14, 15, 16 and FIG.17 hot enough such that collected oils are able to flow from each of thecollection surfaces. In some cases, it may be desirable to keep the gasstream cooler/condenser colder to facilitate efficient precipitation ofthe volatilized oils into small and or microscopic droplets tofacilitate removal with the centrifugal separation device or centrifugalgas stream mover. In such cases, it may be desirable to keep thesurfaces of the gas stream cooler at about −100 to about −50° F., about−50 to about −25° F., about −25 to about 0° F., about 0 to about 25° F.,about 25 to about 50° F., about 50 to about 75° F., or about 75 to about100° F., or at other temperatures when desirable. The centrifugalcollection device section 83, centrifugal gas stream mover collectionsection 19, electrostatic collection section 84 or filter collectionsection 85 may be kept at a warmer temperature during operation throughactive heating (for example, at one of the warmer temperature rangesdescribed), or may be allowed to assume the temperature of the gasstream after it has passed through the cooler and then be intermittentlyheated during or after operation to facilitate removal of the collectedoils. Additionally, if the gas stream cooler is found to collect oilsthat are too cold to flow, it also may be intermittently heated duringor after operation to allow the collected oils to flow from the gasstream cooler/condenser section 50.

The method may comprise maintaining the temperature of the condensationsurface at about 100° F. to about 300° F., about 110° F. to about 289°F., about 120° F. to about 280° F., about 120° F. to about 150° F.,about 290° F. to about 314° F., about 316° F. to about 355° F., about320° F. to about 340° F., about 357° F. to about 364° F., or about 366°F. to about 427° F. In some embodiments, the method comprisesmaintaining the temperature of the condensation surface at about 100° F.to about 315° F., about 100° F. to about 212° F., or about 120° F. toabout 315° F. The method may comprise maintaining the temperature of thecondensation surface at about 100° F. to about 140° F., about 120° F. toabout 160° F., about 140° F. to about 180° F., about 160° F. to about200° F., about 180° F. to about 220° F., about 200° F. to about 240° F.,about 220° F. to about 260° F., about 240° F. to about 280° F., about260° F. to about 300° F., about 280° F. to about 320° F., about 300° F.to about 340° F., about 320° F. to about 360° F., about 340° F. to about380° F., about 360° F. to about 400° F., about 380° F. to about 420° F.,or about 400° F. to about 440° F.

In some cases, the preferred method may be to keep some condensation orcollection surfaces at different temperatures than other condensation orcollection surfaces. In such cases, any of the temperature ranges inframay be used interchangeably with different components. As a non-limitingexample, it may be preferred to keep the temperature of thecondenser/gas stream cooler 50 within a higher temperature range thanthe centrifugal collection device section 83, centrifugal gas streammover collection section 19, electrostatic collection section 84 orfilter collection section 85, and, in some cases, it may be preferred tokeep the temperature of the condenser/gas stream cooler 50 within alower temperature range than the centrifugal collection device section83, centrifugal gas stream mover collection section 19, electrostaticcollection section 84 or filter collection section 85.

In some embodiments, cooling the gas stream containing the oil comprisescooling the gas stream to a temperature that is at least about 5° F.,10° F., 15° F., 20° F., 25° F., 30° F., 35° F., 40° F., 45° F., or 50°F. lower than the temperature of the condensation surface. Therelatively lower temperature of the gas stream may help condense the gaswhereas the relatively higher temperature of the condensation surfacemay help ensure that the oil remains fluid enough to be collected.Similarly, in some embodiments, cooling the gas stream containing theoil comprises cooling the gas stream to a temperature that is at leastabout 5° F., 10° F., 15° F., 20° F., 25° F., 30° F., 35° F., 40° F., 45°F., or 50° F. higher than the temperature of the condensation surface.The relatively higher temperature of the gas stream may help ensure thatthe oil does not condense prior to contacting the condensation surface.Still, in some embodiments, it may be preferable to cool the gas streamcontaining the oil to a temperature that is about the same temperatureas the temperature of the condensation surface.

A method may comprise changing the temperature of the condensationsurface. For example, a method may comprise increasing the temperatureof the condensation surface. The temperature may be increased todecrease the resistance of the portion of the oil to flow, e.g., toincrease the rate at which the oil is collected from the condensationsurface. The temperature may be increased, for example, in response tooil build-up on the condensation surface. Similarly, a method maycomprise decreasing the temperature of the condensation surface. Thetemperature may be decreased, for example to increase the rate at whichthe condensation surface captures and removes the portion of oil fromthe gas stream.

The method may comprise providing a plant material in the extractionchamber, propelling the gas stream through the extraction chamber, andvolatizing an oil from the plant material such that the oil is extractedfrom the plant material and into the gas stream. In some embodiments,the method may comprise cooling the gas stream containing the oil andpropelling the gas stream containing the oil to the condensationsurface. The method may comprise contacting the gas stream with thecondensation surface thereby capturing and removing a portion of the oilfrom the gas stream. In some embodiments, the method may comprisecollecting the portion of the oil from the condensation surface therebyproducing a collected oil.

In some aspects, the gas stream may comprise less than about 30%, about25%, about 20%, about 15%, about 10%, about 9%, about 8%, about 7%,about 6%, about 5%, about 4%, about 3%, about 2%, or about 1% solventvapor by weight. The gas stream may comprise less than about 30%, about25%, about 20%, about 15%, about 10%, about 9%, about 8%, about 7%,about 6%, about 5%, about 4%, about 3%, about 2%, or about 1% solventvapor by weight prior to propelling the gas stream through theextraction chamber, after propelling the gas stream through theextraction chamber, prior to volatizing the oil, after volatizing theoil, prior to cooling the gas stream, after cooling the gas stream,prior to contacting the gas stream with the condensation surface, aftercontacting the gas stream with the condensation surface, prior tocollecting the portion of oil, and/or after collecting the portion ofoil.

In some aspects, the portion of the oil captured and removed from thegas stream may comprise less than about 30%, about 25%, about 20%, about15%, about 10%, about 9%, about 8%, about 7%, about 6%, about 5%, about4%, about 3%, about 2%, or about 1% solvent by weight. The portion ofthe oil captured and removed from the gas stream may comprise less thanabout 30%, about 25%, about 20%, about 15%, about 10%, about 9%, about8%, about 7%, about 6%, about 5%, about 4%, about 3%, about 2%, or about1% solvent by weight after contacting the gas stream with thecondensation surface, prior to collecting the portion of oil, and/orafter collecting the portion of oil. In some aspects, the collected oilmay comprise less than about 30%, about 25%, about 20%, about 15%, about10%, about 9%, about 8%, about 7%, about 6%, about 5%, about 4%, about3%, about 2%, or about 1% solvent by weight.

It should be noted that in some embodiments, it may be advantageous tointroduce higher ratios of dilution solvent to dilute the collected oilsand prevent the collected oils from becoming too thick to leave thesystem. In such embodiments, the ratio of solvent to oil may beincreased to any higher ratio as needed.

In some aspects, the portion of the oil captured and removed from thegas stream may comprise a dilution solvent to oil ratio of about 25:1 to20:1, about 20:1 to 15:1, about 15:1 to about 10:1, about 10:1, about9:1, about 8:1, about 7:1, about 6:1, about 5:1, about 4:1 about 3:1about 2:1 or about 1:1. The portion of the oil captured and removed fromthe gas stream may comprise a solvent to oil ratio of about 25:1 to20:1, about 20:1 to 15:1, about 15:1 to about 10:1, about 10:1, about9:1, about 8:1, about 7:1, about 6:1, about 5:1, about 4:1 about 3:1about 2:1 or about 1:1 after contacting the gas stream with thecondensation surface, prior to collecting the portion of oil, and/orafter collecting the portion of oil. In some aspects, the collected oilmay comprise a solvent to oil ratio of about 25:1 to 20:1, about 20:1 to15:1, about 15:1 to about 10:1, about 10:1, about 9:1, about 8:1, about7:1, about 6:1, about 5:1, about 4:1 about 3:1 about 2:1 or about 1:1.

In some aspects, the gas stream may comprise a dilution solvent to oilratio of about 25:1 to 20:1, about 20:1 to 15:1, about 15:1 to about10:1, about 10:1, about 9:1, about 8:1, about 7:1, about 6:1, about 5:1,about 4:1 about 3:1 about 2:1 or about 1:1. The gas stream may comprisea solvent to oil ratio of about 25:1 to 20:1, about 20:1 to 15:1, about15:1 to about 10:1, about 10:1, about 9:1, about 8:1, about 7:1, about6:1, about 5:1, about 4:1 about 3:1 about 2:1 or about 1:1 prior topropelling the gas stream through the extraction chamber, afterpropelling the gas stream through the extraction chamber, prior tovolatizing the oil, after volatizing the oil, prior to cooling the gasstream, after cooling the gas stream, prior to contacting the gas streamwith the condensation surface, after contacting the gas stream with thecondensation surface, prior to collecting the portion of oil, and/orafter collecting the portion of oil. The gas stream, portion of the oil,and/or collected oil may comprise little solvent, and/or the gas stream,portion of the oil, or collected oil may be essentially free of solvent.“Essentially free” means that the gas stream, portion of the oil, and/orcollected oil may contain unavoidable impurities from the startingmaterials (e.g., plant material and gas stream) but that the gas stream,portion of the oil, or collected oil are otherwise free from solvent. Insome embodiments, the gas stream, portion of the oil, and/or collectedoil comprise no solvent. The gas stream, portion of the oil, and/orcollected oil may be essentially free of isobutane, ethanol, and/orchloroform.

In some embodiments, contacting the gas stream with the condensationsurface comprises contacting a vapor of the oil with the condensationsurface. Contacting the gas stream with the condensation surface maycause the portion of the oil to condense on the condensation surface.

In some embodiments, the method further comprises condensing the portionof the oil into oil droplets that become entrained in the gas streamafter cooling the gas stream. Contacting the gas stream with thecondensation surface may comprise contacting the oil droplets with thecondensation surface, which may cause the oil droplets to collect on thecondensation surface.

Cooling the gas stream may comprise cooling the gas stream to about 100to about 300° F., about 110 to about 289° F., about 120 to about 280°F., about 120 to about 150° F., about 290 to about 314° F., about 316 toabout 355° F., about 320 to about 340° F., about 357 to about 364° F.,or about 366 to about 427° F. In some embodiments, cooling the gasstream comprises cooling the gas stream to about 98.6 to about 314.6°F., about 98.6 to about 212.0° F., or about 122.0 to about 314.6° F.Cooling the gas stream may comprise cooling the gas stream to about 100°F. to about 140° F., about 120° F. to about 160° F., about 140° F. toabout 180° F., about 160° F. to about 200° F., about 180° F. to about220° F., about 200° F. to about 240° F., about 220° F. to about 260° F.,about 240° F. to about 280° F., about 260° F. to about 300° F., about280° F. to about 320° F., about 300° F. to about 340° F., about 320° F.to about 360° F., about 340° F. to about 380° F., about 360° F. to about400° F., about 380° F. to about 420° F., or about 400° F. to about 440°F. Cooling the gas stream may comprise cooling the gas stream to about−100 to about −50° F., about −50 to about −25° F., about −25 to about 0°F., about 0 to about 25° F., about 25 to about 50° F., about 50 to about75° F., or about 75 to about 100° F.

The method may further comprise heating the gas stream and/or extractionchamber to a temperature higher than the boiling point of at least onemolecule of the portion of oil, e.g., thereby facilitatingvolatilization. Such a temperature may be, for example, about 315° F.,about 356° F., or about 428° F. The temperature higher than the boilingpoint may be about 300° F., about 305° F., about 310° F., about 315° F.,about 320° F., about 325° F., about 330° F., about 335° F., about 340°F., about 345° F., about 350° F., about 355° F., about 360° F., about365° F., about 370° F., about 375° F., about 380° F., about 385° F.,about 390° F., about 395° F., about 400° F., about 405° F., about 410°F., about 415° F., about 420° F., about 425° F., about 430° F., about435° F., about 440° F., about 445° F., about 450° F., or about 460° F.In some embodiments, the at least one molecule may comprise cannabidiol(“CBD”), cannabidivarin (“CBDV”), cannabigerol (“CBG”),delta-9-tetrahydrocannabinol (“THC”), delta-8-tetrahydrocannabinol,tetrahydrocannabivarin (“THCV”), cannabinol (“CBN”), cannabigerol,cannabichromene, a chemically converted cannabinoid, any othercannabinoid, any other terpene or terpenoid, linalool, caryophyllene,myrcene, limonene, humulene, and/or pinene.

The plant material may comprise hemp or cannabis. For example, the plantmaterial may comprise Cannabis sativa, Cannabis indica, Cannabisruderalis, a hybridized cross of a species or family of cannabis, or acombination of two or more of the foregoing.

In some embodiments, the portion of oil and/or collected oil comprisescannabidiol (“CBD”), cannabidivarin (“CBDV”), cannabigerol (“CBG”),delta-9-tetrahydrocannabinol (“THC”), delta-8-tetrahydrocannabinol,tetrahydrocannabivarin (“THCV”), cannabinol (“CBN”), cannabigerol,cannabichromene, a chemically converted cannabinoid, any othercannabinoid, any other terpene or terpenoid, linalool, caryophyllene,myrcene, limonene, humulene, pinene, or a combination of two or more ofthe foregoing. (For example, the portion of oil and/or collected oil maycomprise delta-9-tetrahydrocannabinol (“THC”), e.g., at a weightpercentage of at least about 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%,50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, 95%, or about 99%. Theportion of oil and/or collected oil may comprise cannabidiol (“CBD”),e.g., at a weight percentage of at least about 10%, 15%, 20%, 25%, 30%,35%, 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, 95%, orabout 99%.

Those of skill in the art will recognize that the herein describedembodiments of the present invention may be altered in other wayswithout departing from the scope or teaching of the present invention.As such, this disclosure should be interpreted broadly.

The invention claimed is:
 1. A method to extract an oil from a plantmaterial, comprising: providing the plant material; providing a systemfor extracting the oil from the plant material, wherein the systemcomprises (a) a gas moving device operable to propel a gas streamthrough the system, (b) an extraction chamber in communication with thegas moving device such that the gas stream is directed through theextraction chamber, (c) a condensation surface in communication with thegas moving device such that the gas stream is directed to thecondensation surface; and (d) a plant material separation deviceoperable to separate at least a portion of any plant material that isentrained in the gas stream from the gas stream after the gas streamexits the extraction chamber and before the gas stream is directed tothe condensation surface; feeding the plant material into the extractionchamber; propelling the gas stream through the extraction chamber toentrain the plant material in the gas stream; volatizing the oil fromthe plant material that is entrained in the gas stream such that the oilis extracted from the plant material and into the gas stream; separatingat least a portion of the plant material from the gas stream, whereinthe plant material separation device performs the separating; coolingthe gas stream containing the oil; directing the gas stream containingthe oil to the condensation surface; contacting the gas stream with thecondensation surface to capture and remove a portion of the oil from thegas stream; maintaining the condensation surface at an angle and atemperature that result in a parallel component of gravitational forcethat is greater than the resistance of the portion of the oil to flow;and collecting the portion of the oil from the condensation surface toproduce a collected oil.
 2. The method of claim 1, wherein cooling thegas stream comprises spraying a solvent into the gas stream at a rate ofat least 0.0002 and no greater than 1.0 gallons per minute.
 3. Themethod of claim 2, wherein the gas stream comprises less than 25 percentsolvent vapor by weight.
 4. The method of claim 2, wherein the portionof the oil that is captured and removed from the gas stream comprisesless than 25 percent solvent by weight.
 5. The method of claim 2,wherein the collected oil comprises less than 25 percent solvent byweight.
 6. The method of claim 2, wherein: the collected oil is amixture that comprises the solvent and plant oils; the plant oils have ahigher boiling point than the solvent; and the method further comprisesevaporating the solvent from the collected oil to separate the plantoils from the solvent.
 7. The method of claim 6, wherein evaporating thesolvent comprises applying a vacuum to the collected oil.
 8. The methodof claim 1, further comprising grinding the plant material.
 9. Themethod of claim 1, comprising feeding the plant material into theextraction chamber at a rate of at least 0.03 and no greater than 10pounds per minute.
 10. The method of claim 1, wherein propelling the gasstream through the extraction chamber comprises propelling the gasstream at a rate of at least 30 and no greater than 500 standard cubicfeet per minute.
 11. The method of claim 1, comprising maintaining thecondensation surface at an angle of at least −90 degrees and no greaterthan 60 degrees relative to the force of gravity, wherein: surfaces ofat least −90 degrees and less than 0 degrees are ceilings; surfaces ofexactly 0 degrees are walls that are parallel to the force of gravity;and surfaces of greater than 0 degrees and no greater than 60 degreesare inclined planes.
 12. The method of claim 1, comprising maintainingthe condensation surface at a temperature of at least 100 degreesFahrenheit and no greater than 440 degrees Fahrenheit.
 13. The method ofclaim 1, wherein the condensation surface is a surface of atube-in-shell heat exchanger.
 14. The method of claim 1, whereincollecting the portion of the oil comprises collecting an oleoresin. 15.The method of claim 1, wherein collecting the portion of the oilcomprises collecting a terpene, a terpenoid, or both a terpene and aterpenoid.
 16. The method of claim 15, wherein collecting the portion ofthe oil comprises collecting either linalool, caryophyllene, myrcene,limonene, humulene, pinene, or a combination of two or more of thepreceding molecules.
 17. The method of claim 1, wherein providing theplant material comprises either (i) providing hemp, (ii) providingcannabis, or (iii) providing a composition that comprises either hemp,cannabis, or both hemp and cannabis.
 18. The method of claim 17, whereincollecting the portion of the oil comprises collecting eithercannabigerol, cannabidiol, cannabidivarin, delta-9-tetrahydrocannabinol,tetrahydrocannabivarin, cannabichromene, cannabinol, or two or more ofthe preceding molecules.
 19. A method to extract an oil from a plantmaterial, comprising: providing the plant material, wherein the plantmaterial is either a ground plant material or a powdered plant material;providing a system for extracting the oil from the plant material,wherein the system comprises (a) a gas moving device operable to propela gas stream through the system, (b) an extraction chamber incommunication with the gas moving device such that the gas stream isdirected through the extraction chamber, (c) a condensation surface incommunication with the gas moving device such that the gas stream isdirected to the condensation surface; and (d) a plant materialseparation device operable to separate at least a portion of any plantmaterial that is entrained in the gas stream from the gas stream afterthe gas stream exits the extraction chamber and before the gas stream isdirected to the condensation surface; feeding the plant material intothe extraction chamber at a rate of at least 0.03 and no greater than 10pounds per minute; propelling the gas stream through the extractionchamber to entrain the plant material in the gas stream; volatizing theoil from the plant material that is entrained in the gas stream suchthat the oil is extracted from the plant material and into the gasstream; separating at least a portion of the plant material from the gasstream, wherein the plant material separation device performs theseparating; spraying a solvent into the gas stream at a rate of at least0.0002 and no greater than 1.0 gallons per minute to cool the gas streamcontaining the oil; directing the gas stream containing the oil to thecondensation surface; contacting the gas stream with the condensationsurface to capture and remove a portion of the oil from the gas stream;collecting the portion of the oil from the condensation surface toproduce a collected oil, wherein the collected oil is a mixture thatcomprises the solvent and plant oils; and evaporating the solvent fromthe collected oil to separate the plant oils from the solvent, whereinevaporating the solvent comprises applying a vacuum to the collectedoil.
 20. A method to extract an oil from a plant material, comprising:providing the plant material; providing a system for extracting the oilfrom the plant material, wherein the system comprises (a) a gas movingdevice operable to propel a gas stream through the system, (b) anextraction chamber in communication with the gas moving device such thatthe gas stream is directed through the extraction chamber, (c) acondensation surface in communication with the gas moving device suchthat the gas stream is directed to the condensation surface; and (d) aplant material separation device operable to separate at least a portionof any plant material that is entrained in the gas stream from the gasstream after the gas stream exits the extraction chamber and before thegas stream is directed to the condensation surface; grinding the plantmaterial to convert the plant material into a ground plant material;feeding the ground plant material into the extraction chamber at a rateof at least 0.03 and no greater than 10 pounds per minute; propellingthe gas stream through the extraction chamber at a rate of at least 30and no greater than 500 standard cubic feet per minute to entrain theground plant material in the gas stream; volatizing the oil from theground plant material that is entrained in the gas stream such that theoil is extracted from the ground plant material and into the gas stream;separating at least a portion of the ground plant material from the gasstream, wherein the plant material separation device performs theseparating; directing the gas stream containing the oil to thecondensation surface; contacting the gas stream with the condensationsurface to capture and remove a portion of the oil from the gas stream;and collecting the portion of the oil from the condensation surface toproduce a collected oil.